TWI359068B - Pelletizing die, pelletizing apparatus and product - Google Patents

Pelletizing die, pelletizing apparatus and product Download PDF

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Publication number
TWI359068B
TWI359068B TW098105224A TW98105224A TWI359068B TW I359068 B TWI359068 B TW I359068B TW 098105224 A TW098105224 A TW 098105224A TW 98105224 A TW98105224 A TW 98105224A TW I359068 B TWI359068 B TW I359068B
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Taiwan
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resin
mold
thermoplastic resin
granulation
particles
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TW098105224A
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Chinese (zh)
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TW200946310A (en
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Yasumasa Asano
Masatoshi Yamashita
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Sekisui Plastics
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B9/00—Making granules
    • B29B9/02—Making granules by dividing preformed material
    • B29B9/06—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion
    • B29B9/065—Making granules by dividing preformed material in the form of filamentary material, e.g. combined with extrusion under-water, e.g. underwater pelletizers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/30—Mixing; Kneading continuous, with mechanical mixing or kneading devices
    • B29B7/58—Component parts, details or accessories; Auxiliary operations
    • B29B7/582—Component parts, details or accessories; Auxiliary operations for discharging, e.g. doors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/80—Component parts, details or accessories; Auxiliary operations
    • B29B7/82—Heating or cooling
    • B29B7/823—Temperature control
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29B—PREPARATION OR PRETREATMENT OF THE MATERIAL TO BE SHAPED; MAKING GRANULES OR PREFORMS; RECOVERY OF PLASTICS OR OTHER CONSTITUENTS OF WASTE MATERIAL CONTAINING PLASTICS
    • B29B7/00—Mixing; Kneading
    • B29B7/80—Component parts, details or accessories; Auxiliary operations
    • B29B7/82—Heating or cooling
    • B29B7/826—Apparatus therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29C—SHAPING OR JOINING OF PLASTICS; SHAPING OF MATERIAL IN A PLASTIC STATE, NOT OTHERWISE PROVIDED FOR; AFTER-TREATMENT OF THE SHAPED PRODUCTS, e.g. REPAIRING
    • B29C44/00—Shaping by internal pressure generated in the material, e.g. swelling or foaming ; Producing porous or cellular expanded plastics articles
    • B29C44/34—Auxiliary operations
    • B29C44/3461—Making or treating expandable particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2023/00—Use of polyalkenes or derivatives thereof as moulding material
    • B29K2023/04—Polymers of ethylene
    • B29K2023/06—PE, i.e. polyethylene
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2023/00—Use of polyalkenes or derivatives thereof as moulding material
    • B29K2023/10—Polymers of propylene
    • B29K2023/12—PP, i.e. polypropylene
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2025/00—Use of polymers of vinyl-aromatic compounds or derivatives thereof as moulding material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2027/00—Use of polyvinylhalogenides or derivatives thereof as moulding material
    • B29K2027/06—PVC, i.e. polyvinylchloride
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2055/00—Use of specific polymers obtained by polymerisation reactions only involving carbon-to-carbon unsaturated bonds, not provided for in a single one of main groups B29K2023/00 - B29K2049/00, e.g. having a vinyl group, as moulding material
    • B29K2055/02—ABS polymers, i.e. acrylonitrile-butadiene-styrene polymers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2101/00—Use of unspecified macromolecular compounds as moulding material
    • B29K2101/12—Thermoplastic materials
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B29—WORKING OF PLASTICS; WORKING OF SUBSTANCES IN A PLASTIC STATE IN GENERAL
    • B29K—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES B29B, B29C OR B29D, RELATING TO MOULDING MATERIALS OR TO MATERIALS FOR MOULDS, REINFORCEMENTS, FILLERS OR PREFORMED PARTS, e.g. INSERTS
    • B29K2105/00—Condition, form or state of moulded material or of the material to be shaped
    • B29K2105/04—Condition, form or state of moulded material or of the material to be shaped cellular or porous
    • B29K2105/048—Expandable particles, beads or granules

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Processing And Handling Of Plastics And Other Materials For Molding In General (AREA)
  • Manufacture Of Porous Articles, And Recovery And Treatment Of Waste Products (AREA)
  • Extrusion Moulding Of Plastics Or The Like (AREA)

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1359068 六、發明說明： 【發明所屬之技術領域】 本發明係關於用以藉由熱切法使熱可塑性樹脂粒子 成形之造粒用模具、造粒裝置及發泡性熱可塑性樹脂粒子 的製造方法。 本申請案係依據2008年2月20日於日本提出申請之 曰本特願2008-39116號主張優先權，並在此援引該内容。 【先前技術】 以往，關於用以使熱可塑性樹脂粒成形之裝置（稱為 製粒機），一般為人所知者，為具備擠壓機、安裝於此擠壓 機的前端之模具、及刀具所構成，將藉由擠壓機進行熔融 捏合後之樹脂材料從模具予以擠出，並以刀具將之切斷而 製造出期望大小的粒之裝置。 關於從模具的噴嘴所擠壓出之樹脂材料的切割法，有 熱切法。 此熱切法，為使複數個喷嘴所開口之模具前端面與循 環水流接觸，並藉由刀具將被剛擠壓出在水流中後的高溫 樹脂予以切斷之方法。於依據熱切法之造粒中，由於在樹 脂還未充分硬化之狀態下進行切斷，所以具有不會產生樹 脂的粉體化，且可獲得球狀粒子等優點。 然而，於熱切法中，由於模具的樹脂吐出面與水流接 觸，所以熱能會在此被水流側奪走，而可能導致模具内部 的溫度部分地降低至樹脂的熔點以下之溫度。結果產生噴 嘴的阻塞，使生產性降低。此外，亦可能因阻塞使粒子的 4 321055 1359068 • 粒徑不一致，導致品質的低落。再者，當阻塞過多時，會 • 有來自模具的樹脂擠壓壓力異常地提高而超出模具的耐壓 .' 極限以致無法進行擠壓的情形。 以往，於依據熱切法之造粒所使用的造粒用模具中， 關於用以防止噴嘴阻塞之技術，例如有專利文獻卜2所揭 示之技術。 於專利文獻1，係揭示一種在配置為圓狀之喷嘴的中 心位置，於與喷嘴的樹脂流路為相同方向配置了棒狀加熱 • 器之造粒用模具。藉由配置棒狀加熱器，使加熱器與各喷 嘴成為等距離，使各喷嘴均一地被加熱。因此，使喷嘴阻 塞不易產生，並可達到低壓力損耗以及在水中之開始擠 壓，而能夠獲得優良的粒。 於專利文獻2，係揭示一種於藉由旋轉刀具，將從模 具所擠壓出之熔融樹脂予以切斷而製得樹脂粒子之熱可塑 性樹脂粒子的製造方法中，於模具表面設置隔熱材之構造。 φ 專利文獻1及2中均進行不含發泡劑之造粒。 專利文獻1:日本特開平7-178726號公報 '專利文獻2:日本特開平5-301218號公報 ‘ 【發明内容】 (發明所欲解決之課題） 然而，於專利文獻1及2所揭示之先前技術中，係存 在下列問題。 亦即，當欲在撥壓機中混合發泡劑來獲得發泡性樹脂 粒子時，必須抑制從模具所吐出之含有發泡劑的樹脂組成 5 321055 1359068 物之發泡。因此，送往切割室（處理室）内之循環水（冷 卻水）的水溫，必須較非發泡樹脂粒子時（8〇至9〇。〇)低 (30至40°C)。此外，由於發泡劑的存在使樹脂的熔融黏 度降低，因此，在不使刀刀接觸（按壓）於模具表面下進 行造粒者’乃變得較困難。 專利文獻1所揭示之先前技術，係以使棒狀加熱器的 前端接近於模具的樹脂吐出面之方式來配置棒狀加熱器， 但棒狀加熱器由於在其構造上無法將鎳克鉻線設置至前端 部為止’所以加熱器前端紐發熱。因此，當對發泡性 脂粒子進行造㈣，於此模具構造中難以將最需要加溫之 模具前端部的樹脂吐出面充分地加溫，所以無法防止阻塞。 此外，於專利文獻2所揭示之先前技術中，記載了未 混合發泡劑之單純的樹脂粒之製造。另一方面，如上所述， 當對發泡性熱可紐樹餘子進行造粒時， 粒時不同，由於需抑制粒子的發泡，所以較理;為= 水的溫度設定在4Gt以下。因此’導致樹脂溫度與循環水 溫度的差擴大’僅Μ熱材並無法充分抑制水流對模具前 端部之熱能的奪走，而容易產生噴嘴的阻塞。此外，如上 所述，於發泡性熱可塑性樹脂粒子的製造時，由於發泡劑 的存在使樹脂軟化，所以必需使刀刃接觸（按壓）於模具 表面來切斷被擠出之樹脂。如專利文獻2所揭示之在以隔 熱材覆蓋表面之模具構造中，隔熱材會因刀料在短時間 内損耗，因而產生模具之耐用性的問題。 本發明係鑒於上述問題而完成之發明，目的在於提供 321055 1359068 - 一種可防止依據熱切法之造粒用模具中之噴嘴的阻塞，而 • 能夠有效率地生產出均勻粒徑的粒子之造粒用模具，造粒 ' 裝置及發泡性熱可塑性樹脂粒子的製造方法。 •(用以解決課題之手段） 為了達成上述目的，於本發明之造粒用模具中，係採 用下列構成。亦即，此造粒用模具，係具備：接觸於冷媒 而設置之樹脂吐出面、連通至樹脂供應裝置之複數個樹脂 流路、與樹脂流路連通且於樹脂吐出面形成開口之喷嘴、 • 以及設置於樹脂吐出面的附近之複數個插裝加熱器 (cartridge heater)。此外，樹脂流路係沿著樹脂吐出面上之 虛擬圓的圓周而配置，插裝加熱器係配置於樹脂流路之圓 周的周方向兩側，並且以使長度方向朝向圓周的徑方向且 貫穿圓周之狀態而配置。 此外，於本發明之造粒用模具中，較佳為插裝加熱器 設置8個以上；各個插裝加熱器的中心角為45° β下。 φ 此外，於本發明之造粒用模具中，較佳為插裝加熱器 設置於距離樹脂吐出面為10至50mm的位置。 w 此外，於本發明之造粒用模具中，較佳為樹脂流路的 '剖面形狀，係於其外輪廓具有直線部；直線部與插裝加熱 器的長度方向大致平行而配置。 此外，於本發明之造粒用模具中，較佳為於樹脂流 路，沿著其剖面形狀設置有複數個噴嘴。 此外，於本發明之造粒用模具中，較佳為至少於冷媒 之水流方向的上游側與下游側設置溫度感測器；且構成為 7 321055 1359068 根據溫度感測器的測定溫度，個別對插裝加熱器進行開關 控制。 此外，本發明之造粒裝置，係具備：上述造粒用模具； 將造粒用模具安裝於前端之樹脂供應裝置；以及收納有將 從造粒用模具的喷嘴所吐出之樹脂予以切斷之刀具，並且 使冷媒與造粒用模具的樹脂吐出面接觸之處理室。 此外，本發明之發泡性熱可塑性樹脂粒子的製造方 法，係具有：將熱可塑性樹脂供應至安裝有上述造粒用模 具之樹脂供應裝置並進行熔融捏合之步驟；一邊使熱可塑 性樹脂朝向造粒用模具移動，一邊將發泡劑注入至熱可塑 性樹脂以形成含有發泡劑的樹脂之步驟；以及藉由刀具， 於冷媒中將從造粒用模具的喷嘴所吐出之含有發泡劑的樹 脂予以切斷，而製得發泡性熱可塑性樹脂粒子之步驟。 .此外，於本發明之發泡性熱可塑性樹脂粒子的製造方 法中，較佳為至少測定冷媒之水流方向的上游側與下游側 之模具溫度，並且以使各個測定值成為相等之方式，個別 對各插裝加熱器進行開關控制。 此外，本發明之熱可塑性樹脂發泡粒子的製造方法， 係具有：將熱可塑性樹脂供應至安裝有上述造粒用模具之 樹脂供應裝置並進行熔融捏合之步驟；一邊使熱可塑性樹 脂朝向造粒用模具移動，一邊將發泡劑注入至熱可塑性樹 脂以形成含有發泡劑的樹脂之步驟；藉由刀具，於冷媒中 將從造粒用模具的喷嘴所吐出之含有發泡劑的樹脂予以切 斷，而製得發泡性熱可塑性樹脂粒子之步驟；以及使發泡 8 321055 1359068 • 性熱可塑性樹脂粒子預發泡，而製得熱可塑性樹脂發泡粒 • 子之步驟。 此外，本發明之熱可塑性樹脂發泡成形體的製造方 法，係具有：將熱可塑性樹脂供應至安裝有上述造粒用模 具之樹脂供應裝置並進行熔融捏合之步驟；一邊使熱可塑 性樹脂朝向造粒用模具移動，一邊將發泡劑注入至熱可塑 性樹脂以形成含有發泡劑的樹脂之步驟；藉由刀具，於冷 媒中將從造粒用模具的喷嘴所吐出之含有發泡劑的樹脂予 • 以切斷，而製得發泡性熱可塑性樹脂粒子之步驟；加熱發 ‘ 泡性熱可塑性樹脂粒子以使其預發泡，而製得熱可塑性樹 # 脂發泡粒子之步驟；以及使熱可塑性樹脂發泡粒子於模内 發泡成形，而製得熱可塑性樹脂發泡成形體之步驟。 此外，本發明之發泡性熱可塑性樹脂粒子，為藉由上 述發泡性熱可塑性樹脂粒子的製造方法所製得之發泡性熱 可塑性樹脂粒子。 φ 此外，本發明之熱可塑性樹脂發泡粒子，為使上述發 泡性熱可塑性樹脂粒子預發泡所製得之熱可塑性樹脂發泡 • 粒子。 '此外，本發明之熱可塑性樹脂發泡成形體，為使上述 熱可塑性樹脂發泡粒子於模内發泡成形所製得之熱可塑性 樹脂發泡成形體。 (發明之效果） 根據本發明之造粒用模具，造粒裝置及發泡性熱可塑 性樹脂粒子的製造方法，樹脂流路及喷嘴係在藉由插裝加 9 321055 1359068 熱斋從兩側夾持之狀態下被加熱。所以不會僅加熱樹脂流 路的單側，而能夠從兩側以等距離均等地加熱。結果可抑 制噴嘴的阻塞，改善因阻塞所導致之生產效率的降低，並 製造出均勻粒徑的高品質粒子。 【實施方式】 生以下係根據第1圖至第4圖，說明本發明實施形態之 造粒用模具，造粒裝置及發泡性熱可塑性樹脂粒子的製造 方法。 t 第1圖為本發明實施形態之造粒裝置之構成圖，第2 圖為顯示本發明實施形態之造粒用模具的概略構成之側剖 面圖’第3圖為顯示第2圖之模具本體的樹腊吐出面之側 視圖，第4圖為顯示喷嘴之配置狀態的一例圖。 •如第1圖及第2圖所示，本實施形態之造粒裝置丁， ，藉由水中熱财式進行造粒之造粒裝置，係採用本發明 實施形態之造粒用模具j。 本造粒裝置T係具備：將造粒用模具1安裝於前端之 擠C機（¼脂供應裝置）2 ;以及收納用以將從造粒用模具 1的喷匕嘴15所吐出之樹脂（於本實施形態中為含有發泡劑 、樹月曰0 )予以切畊之刀具3，並且用以使水流接觸於造 粒用模具1的樹脂吐出面13之處理室4。於處理室4連接 ^用以使痛環水流通之管路5，此管路5的一端（較處理 •上為側）係經介送水栗浦6而連接於水槽7。此外， ;I路的另柒（較處理室4下游側），設置有從循環水 中分離出發泡性熱可塑性樹脂粒子，並進行脫水、乾燥之 321055 10 1359068 • 脫水處理部8。於該脫水處理部8被分離且經脫水、乾燥 ' 後之發泡性熱可塑性樹脂粒子，被送至容器9。圖號21為 .供料斗，22為發泡劑供應口，23為高塵泵浦。 以下說明中係統一下列用詞，於造粒裝置T及造粒用 模具1中，係以吐出樹脂的一側為「前方」、「前端」，以該 相反側為「後方」、「後端」。 如第2圖及第3圖所示，造粒用模具1係由模具本體 10以及固定於擠壓機2的前端侧（圖中右側）之模具固持 • 器11所形成，模具本體10藉由複數個螺栓12、12、…被 固定於模具固持器11的前端側。 模具固持器11係連通於擠壓機2的缸體而設置，並 從後端側朝向前端侧依序形成有後端側流路11a、前端側 流路lib。模具本體10於後端面中央部係形成有往後方側 突出而成之圓錐狀凸部10a，在模具本體10與模具固持器 11為連接之狀態下，於模具固持器11的前端側流路lib φ 内，隔著預定間隙插入有圓錐狀凸部10a。亦即，通過模 具固持器11的後端側流路11a之含有發泡劑的樹脂20， ' 係於前端側流路lib沿著圓錐狀凸部10a的周面流動，並 流入在模具本體10的後端面形成開口之複數個樹脂流路 14、14、…（後述）。 模具本體10係具備：於其前端面與水流接觸之樹脂 吐出面13 ;用以將從擠壓機2所擠壓出之含有發泡劑的樹 脂20朝向樹脂吐出面13移送之複數個樹脂流路14、 14、…；設置於複數個樹脂流路14、14、…的前端且於樹 11 321055 1359068 月曰吐出面13形成開口之複數個嗔嘴15、15、...；設置於 樹月曰吐出面13的中心位置之隔熱材16 ;在較樹脂吐出面 ^更ϋ㈣機2側的位置用以加熱樹脂吐出自13或樹脂 之插裝加熱器17;以及用以加熱模具本體之短 加熱器18而概略地構成。 插裝加熱Is Π及短加熱器18，可因應模具本體 的大小杨狀’從以往所知的插裝加熱器巾適當地選擇來 使用。亦即，以插裝加熱器17及短加熱器18而言，可使 用例如將捲繞於棒狀陶免之發熱線（錄克鉻線）插入於管 (财熱不鐵鋼）中’並且以高熱傳導性與高絕緣性優良之 材料（MgO)來密封發熱線與管之間的間隙而成之電力密 度高的棒狀加熱器。 插裝加熱器17及短加熱g 18，可為在單側具有二條 引線之插裝加熱器，或是在兩側分別具有i條引線之插裝 加熱器（護套加熱器），但在單側具有2條引線之插裝加熱 裔的電力禮度較局’因而較佳。 於模具本體10之樹脂吐出面13的中心部，係配置有 圓形剖面的隔熱材16,並於該隔熱材16的徑方向外側沿 著同心圓設置複數個噴嘴15、15、··.的吐出口。配置有： 熱材16及喷嘴15、15、…之樹脂吐出面13的中央部分， 係於處理室4内部與水接觸。 樹脂流路14、U、...係呈圓形剖面，並延伸存在於與 樹脂吐出δ 13直交之方向’且沿著以模具本體1〇的中二 軸線為中心之圓周（樹脂吐出面13上之虛擬圓的圓周^ 321055 12 1359068 •著一定的間隔而配置。於本實施形態中，樹脂流路14 ' • 14、…係设置於8處，且於前述圓周的周方向上互為鄰接 .之樹脂流路14、14彼此的中心角為45«。如上所述，各樹 月曰ΛΙΙ_路14係連通於模具固持器1 1的前端側流路1 lb。 i嘴15、15、…係沿著樹脂吐出面13上之虛擬圓的 圓周，隔著預定間隔而配置。如第4圖所示，具體而言， 一處的喷嘴15係在樹脂流路14之剖面形狀的範圍内任意 配置了複數個單體噴嘴15a、15b、15c、…而構成喷嘴單 參元（於本發明中將此稱為「噴嘴」）。各單體噴嘴15a、15b、 15c、…的配置方法，可採用例如於複數個小圓周上排列多 數個等方式，但並不限定於此配置形態。 隔熱材16係設置於配置了複數個喷嘴Μ、15、…之 圓周内側的樹脂吐出面13,並以不會使模具本體1〇的熱 月b逸散至處理室4内的水之方式，來抑制模具本體1〇的溫 度降低。以此隔熱材16而言，較理想為使用具有耐水性， •且表面硬度較高之構造的隔熱材。可使用例如，配置即使 與同’皿的模具本體10接觸亦不會引起變形等之耐熱性能 I及隔熱性能優良的隔熱材，並以隔熱性能優良之氟樹脂等 防水性樹脂被覆此隔熱材，然後於樹脂吐出面13侧，依序 層合不鏽鋼、陶瓷等表面硬度高的材料之層合型隔熱材 16° 插裝加熱器17及短加熱器18係分別形成棒狀加熱 器，插裝加熱器17相較於短加熱器18，係位在造粒用模 具1的前端後端方向之樹脂吐出面13側。 321055 13 1359068 插裝加熱器17、17、…係配置於樹脂流路14之前述 圓周的周方向兩側，並且以使長度方向朝向圓周的徑方向 且橫穿該圓周之狀態而配置，具有於樹脂吐出面13的附 近，可加熱樹脂吐出面13、喷嘴15、及樹脂流路14之功 能。本實施形態之插裝加熱器17、17、…，係分別於圓周 方向具有預定的中心角（在此為45°的角度）而設置有8 個。 亦即，各個喷嘴15係藉由2個插裝加熱器17、17， 從前述圓周的周方向予以夾持而配置。 此外，插裝加熱器17係設於樹脂吐出面13的附近， 亦即設在從樹脂吐出面13朝向擠壓機2側距預定的加熱器 深度範圍内。在此，所謂的加熱器深度，是指從樹脂吐出 面13至‘表面加熱用之插裝加熱器17的中心部為止之距離 (第2圖所示之圖號L)，係顯示插裝加熱器17離樹脂吐 出面之位置。關於加熱器深度，在不會對模具的加工面或 耐久性造成阻礙之範圍内，該距離愈小者，噴嘴的阻塞抑 制效果愈大，因而較為理想。亦即，加熱器深度較理想為 10至50mm的範圍。當未滿10mm時，可能對模具的加工 面或耐久性造成阻礙，當超過50mm時，喷嘴的阻塞抑制 效果可能會降低。更理想的範圍為15至30mm。 再者，插裝加熱器17的直徑，在可確保發熱容量的 範圍内，較小者可使樹脂流路的剖面積獲得加大，並且喷 嘴數亦較多，因而較為理想。亦即，以插裝加熱器17的直 徑而言，較理想為15mm以下，但當未滿10mm時，難以 14 321055 1359068 •確保所需的發熱容量’並且加熱器變得較昂貴，所以較理 ，想為10mm至15mm，更理想為1〇mffl至12mm。 • 插裝加熱器17的長度，係設定為在模具本體1〇的半 '徑方向，從較所配置的嘴冑^更往中心側延伸之位置（亦 即，至少使插裝加熱H 17的前端部較喷嘴15 t往中心側 之位置）開始至模具本體1〇 #大致外周為止的位置。 短加熱器18、18、…係對各插裝加熱器卩隔著預定 間隔配置於後方側，配置有與插裝加熱器n的個數為相同 數目（8個），為具有加熱樹脂流路14的後端側之功能。 短加熱器18的長度較插裝加熱器17短。 此外，於模具本體10，在接近於樹脂吐出面13的位 置，於上下左右的4處設置有熱電偶等測溫體19 〇9a、 19B、19C、19D)(溫度感測器）。亦即，係構成為根據這 些測溫體19的測定溫度個別地對插裂加熱器17進行開關 控制，而能夠進行模具本體10的溫度調整。此外，測溫體 着19的没置位置’較理想為位於樹脂吐出面13後方且位於 插裝加熱器17前方。設置場所並不限定於上下左右的4 •處，亦可為上下的2處。再者，較理想為在短加熱器18 的附近設置短加熱器18的溫度控制用之另一個測溫體”， (參考第2圖）。 接著說明使用安裝了上述造粒用模具i之造粒裝置τ 之發泡性熱可塑性樹脂粒子、熱可塑性樹脂發泡粒子、及 熱可塑性樹脂發泡成形體的製造方法。 第1圖所示之造粒裝置T中所使用的擠壓機2 (樹脂 321055 15 1359068 供應裝置）’可因應所造粒之樹脂的種類等，從以往所 各種擠壓機中適當地選擇而使用，可採用例如使用螺椁之 擠壓機或未使用螺桿之擠壓機。使用螺桿之擠壓機，例如 有單軸式擠壓機、多轴式播壓機、通氣式擠壓機、串聯式 擠壓機等。此外’未使用螺桿之擠壓機，例如有柱塞式^ 壓機、齒輪系浦式擠壓機等。此外，任—_壓機& = 用靜態摻合機。這些擠壓機中，就生產性的方面來看，較 理想為使用螺桿之擠壓機。此外，收納了刀具3之處理= 4，亦可使用熱切法中所使用之一般所知者。 於本發明中，熱可塑性樹脂的種類並無特別限定，惟 例如可使用聚苯乙烯系樹脂、聚乙烯系樹脂、聚丙婦系樹 脂、聚醋系樹脂、氣乙烯系樹脂、ABS樹脂、^樹脂等、 或是混合2種以上而使用。亦可使用從曾經用作為樹脂製 品者所回收而製得之熱可塑性樹脂的回收樹脂。尤其理想 為使用聚苯乙稀（GPPS ; General-Purpose P〇IyStyrene :通 用級聚苯乙烯）、耐衝擊聚苯乙烯（mps ·1. Technical Field of the Invention The present invention relates to a granulation mold, a granulation apparatus, and a method for producing foamable thermoplastic resin particles for forming thermoplastic resin particles by a hot cutting method. The present application claims priority based on Japanese Patent Application No. 2008-39116, filed on Jan. [Prior Art] Conventionally, a device for forming a thermoplastic resin pellet (referred to as a granulator) is generally known as an extruder, a mold attached to the tip end of the extruder, and The cutter is constructed by extruding a resin material which is melt-kneaded by an extruder from a die and cutting it with a cutter to produce a pellet of a desired size. Regarding the cutting method of the resin material extruded from the nozzle of the mold, there is a hot cutting method. This hot cutting method is a method in which a front end surface of a mold opened by a plurality of nozzles is brought into contact with a circulating water flow, and a high temperature resin which has just been extruded into a water flow is cut by a cutter. In the granulation by the hot cutting method, since the cutting is performed in a state where the resin is not sufficiently cured, there is an advantage that the resin is not powdered and spherical particles can be obtained. However, in the hot cutting method, since the resin discharge surface of the mold comes into contact with the water flow, the heat energy is taken away by the water flow side, and the temperature inside the mold may be partially lowered to a temperature lower than the melting point of the resin. As a result, the nozzle is clogged, which reduces productivity. In addition, it may also cause the particle size of 4 321055 1359068 • particle size to be inconsistent due to blockage, resulting in low quality. Furthermore, when there is too much clogging, there is a case where the resin extrusion pressure from the mold is abnormally increased beyond the pressure resistance of the mold. The limit is such that the extrusion cannot be performed. In the granulation mold used for granulation by the hot cutting method, for example, a technique for preventing nozzle clogging is disclosed, for example, in the technique disclosed in Patent Document 2. Patent Document 1 discloses a granulation mold in which a rod-shaped heater is disposed in the same direction as a resin flow path of a nozzle in a center position of a nozzle arranged in a circular shape. By arranging the rod heaters, the heaters are equidistant from the respective nozzles, so that the nozzles are uniformly heated. Therefore, nozzle clogging is less likely to occur, and low pressure loss and initial squeezing in water can be achieved, and excellent granules can be obtained. Patent Document 2 discloses a method for producing a thermoplastic resin particle obtained by cutting a molten resin extruded from a mold by a rotary cutter to obtain resin particles, and a heat insulating material is provided on the surface of the mold. structure. φ In Patent Documents 1 and 2, granulation without a foaming agent is carried out. [Patent Document 2: Japanese Laid-Open Patent Publication No. Hei No. 5-301218] In the technology, the following problems exist. That is, when it is desired to mix the foaming agent in the press to obtain the expandable resin particles, it is necessary to suppress the foaming of the resin composition 5 321055 1359068 which is discharged from the mold. Therefore, the water temperature of the circulating water (cooling water) sent to the cutting chamber (processing chamber) must be lower than that of the non-foamed resin particles (8 to 9 Torr) (30 to 40 ° C). Further, since the melt viscosity of the resin is lowered by the presence of the foaming agent, it becomes difficult to carry out the granulation without bringing the blade into contact with (pressing) the surface of the mold. In the prior art disclosed in Patent Document 1, the rod heater is disposed such that the tip end of the rod heater is close to the resin discharge surface of the mold, but the rod heater cannot be made of nickel chrome wire because of its structure. Set to the front end section so the heater front end heats up. Therefore, when the foamable lipid particles are produced (4), it is difficult to sufficiently heat the resin discharge surface of the tip end portion of the mold which is most required to be heated in this mold structure, so that clogging cannot be prevented. Further, in the prior art disclosed in Patent Document 2, the production of a simple resin pellet of an unmixed foaming agent is described. On the other hand, as described above, when the foaming thermocomposite is granulated, the granules are different, and it is preferable to suppress the foaming of the particles; the temperature of the water is set to be 4 Gt or less. Therefore, the difference between the temperature of the resin and the temperature of the circulating water is increased. Only the hot material does not sufficiently suppress the heat loss of the water at the front end portion of the mold, and the nozzle is likely to be clogged. Further, as described above, in the production of the foamable thermoplastic resin particles, the resin is softened by the presence of the foaming agent, so that it is necessary to contact (press) the blade against the surface of the mold to cut the extruded resin. As disclosed in Patent Document 2, in a mold structure in which a surface is covered with a heat insulating material, the heat insulating material is lost in a short time due to the blade material, thereby causing a problem of durability of the mold. The present invention has been made in view of the above problems, and an object thereof is to provide 321055 1359068 - a clogging preventing nozzles in a granulation mold according to a hot cutting method, and capable of efficiently producing granules of particles having a uniform particle size A method of producing a device and a foamable thermoplastic resin particle by a mold. (Means for Solving the Problem) In order to achieve the above object, the granulation mold of the present invention has the following constitution. In other words, the granulation mold includes a resin discharge surface that is provided in contact with the refrigerant, a plurality of resin flow paths that communicate with the resin supply device, and a nozzle that communicates with the resin flow path and forms an opening in the resin discharge surface. And a plurality of cartridge heaters disposed in the vicinity of the resin discharge surface. Further, the resin flow path is disposed along the circumference of the virtual circle on the resin discharge surface, and the insertion heater is disposed on both sides in the circumferential direction of the circumference of the resin flow path, and penetrates in the radial direction of the circumferential direction in the longitudinal direction. Configured in the state of the circumference. Further, in the granulation mold of the present invention, it is preferable to provide eight or more cartridge heaters; the center angle of each of the cartridge heaters is 45° β. φ Further, in the granulation mold of the present invention, it is preferable that the insertion heater is provided at a position of 10 to 50 mm from the resin discharge surface. Further, in the granulating mold of the present invention, it is preferable that the cross-sectional shape of the resin flow path has a straight portion formed on the outer contour thereof, and the straight portion is disposed substantially parallel to the longitudinal direction of the insert heater. Further, in the granulation mold of the present invention, it is preferable that a plurality of nozzles are provided along the cross-sectional shape of the resin flow path. Further, in the granulating mold of the present invention, it is preferable that a temperature sensor is provided at least on the upstream side and the downstream side in the flow direction of the refrigerant; and the configuration is 7 321055 1359068, depending on the measured temperature of the temperature sensor, individual pairs The plug-in heater is used for switching control. In addition, the granulation apparatus of the present invention includes: the granulation mold; the resin supply device that mounts the granulation mold to the tip; and the resin that is discharged from the nozzle of the granulation mold is cut. The cutter and the processing chamber in which the refrigerant is brought into contact with the resin discharge surface of the granulation mold. Further, the method for producing the foamable thermoplastic resin particles of the present invention comprises the steps of: supplying a thermoplastic resin to a resin supply device to which the granulation mold is attached, and performing melt-kneading; a step of moving a pellet by a mold, injecting a foaming agent into a thermoplastic resin to form a resin containing a foaming agent, and a foaming agent which is discharged from a nozzle of the granulating mold in a refrigerant by a cutter. The step of cutting off the resin to obtain foamable thermoplastic resin particles. Further, in the method for producing the foamable thermoplastic resin particles of the present invention, it is preferred to measure at least the mold temperature on the upstream side and the downstream side in the water flow direction of the refrigerant, and to make the respective measured values equal. Switch control is performed for each cartridge heater. Further, the method for producing the thermoplastic resin expanded particles of the present invention comprises the steps of: supplying a thermoplastic resin to a resin supply device to which the granulation mold is attached and performing melt-kneading; and directing the thermoplastic resin toward granulation a step of injecting a foaming agent into a thermoplastic resin to form a resin containing a foaming agent by moving a mold; and a resin containing a foaming agent discharged from a nozzle of the granulating mold in a refrigerant by a cutter The step of cutting off the foamed thermoplastic resin particles and the step of pre-expanding the foamed thermoplastic resin particles by foaming 8321055 1359068 to obtain the thermoplastic resin foamed particles. Further, the method for producing a thermoplastic resin foam molded article of the present invention comprises the steps of: supplying a thermoplastic resin to a resin supply device to which the granulation mold is attached, and performing melt-kneading; a step of moving a pellet by a mold, injecting a foaming agent into a thermoplastic resin to form a resin containing a foaming agent, and a resin containing a foaming agent discharged from a nozzle of the granulating mold in a refrigerant by a cutter The step of preparing the foamable thermoplastic resin particles by cutting, heating the foaming thermoplastic resin particles to pre-expand them, and preparing the thermoplastic foam tree #脂泡沫颗粒颗粒; The thermoplastic resin foamed particles are subjected to foam molding in an in-mold to obtain a thermoplastic resin foam molded body. Further, the foamable thermoplastic resin particles of the present invention are foamable thermoplastic resin particles obtained by the above-described method for producing foamable thermoplastic resin particles. Further, the thermoplastic resin foamed particles of the present invention are foamed particles of a thermoplastic resin obtained by pre-expanding the above-mentioned foamable thermoplastic resin particles. Further, the thermoplastic resin foam molded article of the present invention is a thermoplastic resin foam molded article obtained by foam molding the above-mentioned thermoplastic resin foamed particles in an in-mold. (Effect of the Invention) According to the granulation mold of the present invention, the granulation apparatus and the method for producing the foamable thermoplastic resin particles, the resin flow path and the nozzle are clamped by both sides by means of inserting and adding 9 321055 1359068 It is heated while being held. Therefore, it is not necessary to heat only one side of the resin flow path, and it is possible to uniformly heat from both sides at equal distances. As a result, nozzle clogging can be suppressed, the production efficiency due to clogging can be improved, and high-quality particles of uniform particle size can be produced. [Embodiment] The granulation mold, the granulation device, and the method for producing the foamable thermoplastic resin particles according to the embodiment of the present invention will be described below with reference to Figs. 1 to 4 . 1 is a configuration diagram of a granulation apparatus according to an embodiment of the present invention, and FIG. 2 is a side cross-sectional view showing a schematic configuration of a granulation mold according to an embodiment of the present invention. FIG. 3 is a view showing a mold body of FIG. A side view of the tree wax discharge surface, and Fig. 4 is a view showing an example of the arrangement state of the nozzle. As shown in Fig. 1 and Fig. 2, the granulation apparatus of the present embodiment is a granulation apparatus for granulation by the hot water type in the water, and the granulation mold j of the embodiment of the present invention is used. The granulation apparatus T includes a C (a grease supply device) 2 that mounts the granulation mold 1 at the tip end, and a resin that is discharged from the squirt 15 of the granulation mold 1 ( In the present embodiment, the cutter 3 which is subjected to the cutting of the foaming agent and the tree stalk is used, and the water is brought into contact with the processing chamber 4 of the resin discharge surface 13 of the granule 1 for granulation. A pipe 5 for circulating the pain ring water is connected to the processing chamber 4, and one end (the side on the upper side of the process) is connected to the water tank 7 via the water pump 6 . Further, the other side of the I path (the downstream side of the processing chamber 4) is provided with a foamable thermoplastic resin particle separated from the circulating water, and dehydrated and dried. 321055 10 1359068 • Dehydration treatment unit 8. The foamable thermoplastic resin particles separated from the dewatering treatment unit 8 and dehydrated and dried are sent to the container 9. Figure 21 is a supply hopper, 22 is a blowing agent supply port, and 23 is a high dust pump. In the following description, in the granulator T and the granulation mold 1, the side where the resin is discharged is "front" and "front end", and the opposite side is "rear" and "back". "." As shown in Figs. 2 and 3, the granulating mold 1 is formed by a mold main body 10 and a mold holding device 11 fixed to the front end side (the right side in the drawing) of the extruder 2, and the mold main body 10 is used. A plurality of bolts 12, 12, ... are fixed to the front end side of the mold holder 11. The mold holder 11 is provided in communication with the cylinder of the extruder 2, and the rear end side flow path 11a and the front end side flow path lib are sequentially formed from the rear end side toward the front end side. In the mold main body 10, a conical convex portion 10a projecting toward the rear side is formed in the center portion of the rear end surface, and the flow path lib is formed on the front end side of the mold holder 11 in a state where the mold main body 10 and the mold holder 11 are connected to each other. In the φ, the conical convex portion 10a is inserted through a predetermined gap. In other words, the resin 20 containing the foaming agent in the rear end side flow path 11a of the mold holder 11 flows along the circumferential surface of the conical convex portion 10a and flows into the mold body 10 The rear end surface forms a plurality of resin flow paths 14, 14, ... (described later). The mold main body 10 includes a resin discharge surface 13 that is in contact with the water flow at the front end surface thereof, and a plurality of resin flows for transferring the resin 20 containing the foaming agent extruded from the extruder 2 toward the resin discharge surface 13. Roads 14, 14, ...; a plurality of nozzles 15, 15, ... disposed at the front end of the plurality of resin flow paths 14, 14, ... and forming an opening in the tree 11 321055 1359068 The heat insulating material 16 at the center of the surface of the moon squirting surface 13 is used to heat the resin to discharge the insert heater 17 from the resin or the resin at a position on the side of the resin (2) machine 2; and to heat the mold body The heater 18 is configured to be short. The cartridge heating Is Π and the short heater 18 can be appropriately selected from conventionally known cartridge heaters in accordance with the size of the mold body. That is, in the case of the cartridge heater 17 and the short heater 18, for example, a heating wire (coke chrome wire) wound around a rod-shaped pottery can be inserted into a tube (in the case of a non-ferrous steel). A rod-shaped heater having a high power density by sealing a gap between a heating wire and a tube with a material having high thermal conductivity and high insulating property (MgO). The cartridge heater 17 and the short heating g 18 may be an interposer heater having two leads on one side or an interposer heater (sheath heater) having i leads on both sides, but in a single The power of the plug-in heating person with 2 leads on the side is better than the current one. A heat insulating material 16 having a circular cross section is disposed at a central portion of the resin discharge surface 13 of the mold main body 10, and a plurality of nozzles 15, 15, ... are disposed along the concentric circle on the outer side in the radial direction of the heat insulating material 16. The spit out. The central portion of the resin discharge surface 13 of the hot material 16 and the nozzles 15, 15, ... is placed in contact with water inside the processing chamber 4. The resin flow paths 14, U, ... have a circular cross section and extend in a direction orthogonal to the resin discharge δ 13 and along a circumference centering on the center two axes of the mold body 1 ( (resin discharge surface 13) Circumference of the upper virtual circle ^ 321055 12 1359068 • Arranged at a certain interval. In the present embodiment, the resin flow paths 14', 14, ... are provided at eight places, and are adjacent to each other in the circumferential direction of the circumference. The central angles of the resin flow paths 14 and 14 are 45 «. As described above, each of the tree rafts 14 is connected to the front end side flow path 1 lb of the mold holder 1 1. The nozzles 15, 15 The arrangement is arranged along the circumference of the virtual circle on the resin discharge surface 13 at predetermined intervals. As shown in Fig. 4, specifically, the nozzle 15 at one place is within the range of the cross-sectional shape of the resin flow path 14. A plurality of unit nozzles 15a, 15b, 15c, ... are arbitrarily arranged to constitute a nozzle single-element (referred to as "nozzle" in the present invention). A method of arranging the individual nozzles 15a, 15b, 15c, ..., For example, a plurality of ways may be arranged on a plurality of small circumferences, but the present invention is not limited thereto. The heat insulating material 16 is disposed on the resin discharge surface 13 on the inner side of the circumference of the plurality of nozzles 15, 15, ..., and is discharged into the processing chamber 4 without causing the heat of the mold body 1 to escape. In the case of the water, it is preferable to use a heat insulating material having a structure having water resistance and a high surface hardness, and it is preferable to use, for example, even if the heat insulating material 16 is used. The heat-resistant material I and the heat-insulating material excellent in heat-insulating property, such as a fluororesin which is excellent in heat-insulating property, are coated with the heat-resistant material such as a fluororesin which is excellent in heat-insulating property, and is then contacted with the mold body 10 of the same dish. On the side of the resin discharge surface 13, a laminated heat insulating material having a high surface hardness such as stainless steel or ceramics is laminated in this order. The plug heater 17 and the short heater 18 are respectively formed into rod heaters, and the heaters are inserted. 17 is compared with the short heater 18 at the resin discharge surface 13 side of the front end rear end direction of the granulation mold 1. 321055 13 1359068 The insertion heaters 17, 17, ... are disposed in the resin flow path 14 as described above. Both sides of the circumference of the circumference, and to make the length It is disposed in a state of being oriented in the radial direction of the circumference and crossing the circumference, and has a function of heating the resin discharge surface 13, the nozzle 15, and the resin flow path 14 in the vicinity of the resin discharge surface 13. The insertion heating of the embodiment The devices 17, 17, ... are respectively provided with a predetermined central angle (here, an angle of 45°) in the circumferential direction. In other words, each nozzle 15 is provided by two cartridge heaters 17, 17 The arranging heater 17 is disposed in the vicinity of the resin discharge surface 13, that is, in the vicinity of the resin discharge surface 13 toward the extruder 2 by a predetermined heater. Within the depth range. Here, the term "heater depth" refers to the distance from the resin discharge surface 13 to the center portion of the surface heating heater 17 (the figure L shown in Fig. 2), and shows the insertion heating. The position of the device 17 from the resin discharge surface. Regarding the depth of the heater, it is preferable that the smaller the distance is, the larger the blocking inhibition effect of the nozzle is, in the range which does not hinder the processing surface or durability of the mold. That is, the heater depth is desirably in the range of 10 to 50 mm. When it is less than 10 mm, it may hinder the processing surface or durability of the mold. When it exceeds 50 mm, the nozzle suppression effect may be lowered. A more desirable range is 15 to 30 mm. Further, the diameter of the cartridge heater 17 is preferably within a range in which the heat generation capacity can be secured, and the smaller the cross-sectional area of the resin flow path can be increased, and the number of nozzles is also large. That is, in terms of the diameter of the cartridge heater 17, it is preferably 15 mm or less, but when it is less than 10 mm, it is difficult to 14 321055 1359068. • The required heat capacity is ensured and the heater becomes expensive, so it is reasonable. I think it is 10mm to 15mm, more preferably 1〇mffl to 12mm. • The length of the cartridge heater 17 is set to a position extending from the more disposed nozzle 往 to the center side in the half-diameter direction of the mold body 1 (ie, at least the insertion heating H 17 The front end portion is located closer to the center of the mold body 1 〇 than the nozzle 15 t toward the center side. The short heaters 18, 18, ... are disposed on the rear side with respect to the respective insertion heaters at predetermined intervals, and are disposed in the same number (eight) as the number of the insertion heaters n, and have a heating resin flow path. The function of the back end side of 14. The length of the short heater 18 is shorter than that of the cartridge heater 17. Further, in the mold main body 10, temperature measuring bodies 19 〇 9a, 19B, 19C, and 19D) (temperature sensors) such as thermocouples are provided at four positions on the upper, lower, left, and right sides in the vicinity of the resin discharge surface 13. In other words, the splitting heater 17 is individually controlled to be switched based on the measured temperatures of the temperature measuring bodies 19, and the temperature of the mold body 10 can be adjusted. Further, the position of the temperature measuring body 19 is desirably located behind the resin discharge surface 13 and in front of the insertion heater 17. The installation location is not limited to 4 locations from top to bottom, left or right, or 2 locations above and below. Further, it is preferable to provide another temperature measuring body for temperature control of the short heater 18 in the vicinity of the short heater 18 (refer to Fig. 2). Next, the use of the above-described granulation mold i is described. The foaming thermoplastic resin particles of the granule device τ, the thermoplastic resin foamed particles, and the method for producing the thermoplastic resin foam molded body. The extruder 2 used in the granulating device T shown in Fig. 1 Resin 321055 15 1359068 "Supply device" can be appropriately selected from various extruders in accordance with the type of resin to be granulated, etc., and can be extruded, for example, using a screw extruder or a screw without using a screw. Extruder using a screw, such as a single-shaft extruder, a multi-axis press, a vented extruder, a tandem extruder, etc. In addition, 'the extruder without a screw, for example Plunger type presses, gear-type pulverizers, etc. In addition, __ presses & = static blenders. These extruders are ideal for productivity. Screw extruder. In addition, where the tool 3 is stored In the present invention, the type of the thermoplastic resin is not particularly limited, and for example, a polystyrene resin, a polyethylene resin, or a polypropylene system can be used. Resin, a polyester resin, an ethylene-based resin, an ABS resin, a resin, or the like may be used in combination of two or more kinds. A recycled resin of a thermoplastic resin obtained by recycling as a resin product may also be used. Especially ideal for the use of polystyrene (GPPS; General-Purpose P〇IyStyrene: general-purpose polystyrene), impact-resistant polystyrene (mps ·

Polystyrene )等聚苯乙烯系樹脂。 聚苯乙烯系樹脂，例如有苯乙婦、α _ f基苯乙烯、 乙烯基甲苯、氯苯乙烯、乙基苯乙烯、異丙基苯乙烯、二 甲基苯乙稀、漠苯乙烯等笨乙烯系單體的單獨聚合物或這 些的共聚物，較理想為含有50質量％以上苯乙烯之聚笨乙 烯系樹脂’更理想為聚苯乙稀。 此外，前述聚苯乙婦系樹脂，可為以前述苯乙烯單體 為主成分之前述苯乙烯系單體以及能夠與此笨乙烯系單體 321055 16 1359068 ‘奚了’、聚口之乙稀單體之共聚物，此乙燐單體例如有（甲 .:)丙烯酸甲醋、（甲基）丙烯酸乙酯、㈤）丙烯酸丁 曰、甲基）丙稀酸十六醋等（甲基）丙稀酸燒基醋；（甲 ‘基）丙稀腈、順丁埽二酸二甲醋、反丁稀二酸二甲醋、反 I烯，酸二乙醋、反丁烯二酸乙醋；此外例如有二乙烯基 本-甲基丙婦酸伸燒二醇醋等之二官能性單體等。 此外，只要是聚苯乙婦系樹脂為主成分’則可添加其 他樹脂、’為了提升發泡成形體的耐衝擊性，所添加的樹脂 例如有添加了聚丁二烯、笨乙烯·丁二烯共聚物、乙烯-丙 非共輛一稀三維共聚物等之二稀系的橡谬狀聚合物之 膠，貝聚笨乙料、樹脂，亦即所謂的耐衝擊聚苯乙婦。 或者疋聚乙稀系樹脂、聚丙烯系樹脂、丙婦酸系樹脂、丙 稀腈-苯乙稀共聚物、丙稀腈·τ二稀-笨乙缚共聚物等。 於本發明之發泡性熱可塑性樹脂粒子中，使用聚苯乙 炸糸樹脂作為熱可塑性樹脂之發泡性聚苯乙婦系樹脂粒 参子’，為原料之聚苯乙蝉系樹脂’除了可使用市售之一般 2聚苯乙婦系樹脂、藉由懸浮聚合法等方法所新製作之聚 苯乙烯系樹脂等之非回收原料的聚苯乙歸系樹脂（以下記 载為非再製聚苯乙歸）之外’亦可使用對使用完畢的聚苯 乙烯系樹脂發泡成形體進行再生處理所製得之回收原料。 此回收原料例如可使用下列回收原料，亦即，回收使用完 畢的聚苯乙烯系樹脂發泡成形體，例如回收裝魚箱、家= 缓衝材、食品包裳角盤等，並藉由擰檬油精溶解方式或加 熱減容積方式予以再生之回收原料。此外，所能夠使^ 321055 .· 17 1359068 回收原料，除了對使用完畢的聚苯乙烯系樹脂發泡成形體 進行再生處理所製得者之外，亦有將從家電製品（例如電 視機、電冰箱、洗衣機、冷氣機等）或事務機器（例如影 印機、傳真機、列印機等）所分別回收之非發泡聚苯乙烯 系樹脂成形體予以粉碎，並進行熔融捏合而重新形成粒狀 而成者。 如第1圖及第2圖所示，當使用上述造粒裝置T來製 造發泡性熱可塑性樹脂粒子時，係將熱可塑性樹脂從供料 斗21供應至在前端安裝了造粒用模具1之擠壓機2,並進 行熔融捏合該樹脂材料。接著一邊將熱可塑性樹脂朝向造 粒用模具1移動，一邊藉由高壓泵浦23，從發泡劑供應口 22將發泡劑壓入至該熱可塑性樹脂，使發泡劑與熱可塑性 樹脂混合而形成含有發泡劑的樹脂20。 含有發泡劑的樹脂20，係從擠壓機2的前端，經由模 具固持器11被傳送至造粒用模具1之模具本體10的樹脂 流路14。通過樹脂流路14所傳送之含有發泡劑的樹脂20, 係從模具本體10的各個喷嘴15被吐出，並藉由刀具2的 旋轉刀刃，於處理室4的水流中（冷媒中）立即被切斷。 如此於處理室4内，被切斷為粒狀之含有發泡劑的樹 脂20，係成為幾乎呈球形的發泡性熱可塑性樹脂粒子。此 發泡性熱可塑性樹脂粒子係隨著水流於管路5内被搬運， 並到達至脫水處理部8，在此從循環水中分離出發泡性熱 可塑性樹脂粒子並進行脫水、乾燥，分離出的水被送至水 槽7。於該脫水處理部8被分離且經脫水、乾燥後之發泡 18 321055 1359068 性熱可塑性樹脂粒子’被傳送至容器9並收納於此容器内^ 前述發泡劑並無特別限定，例如可單獨使用正戊烷、 異戊燒、環戊烧、環戍二蝉等或是混合2種以上而使用。 此外，亦可使用以上述戊烷類為主成分，並混合了正丁烷、 異丁燒、丙鮮者。尤其錢類容易抑制從喷嘴吐出至水 流時之粒子的發泡’因此較為理想。 此外，所謂的發泡性熱可塑性樹脂粒子，是指於熱可 塑性樹脂中含有發㈣，並成形為粒狀，較理想為小球狀 之樹脂粒子。此發泡性熱可塑性樹脂粒子可使用於下述用 途’亦即於自由空間内進行加熱使其預發泡，並將此預發 泡粒子注人於具有期望職賴穴之成賴具的模穴内， 進行蒸氣加錢預發雜子彼祕著後，進行脫模而製造 出期望形狀的發泡樹脂成形品。 接下來說明上述造粒用模具丨的溫度調整方法。 /如第3圖所示，於造粒用模具！的溫度調整方法中， 係將模具本體1G分割為對應於設在樹脂吐出面η附近的 上下左右之測溫體19A、19B、19C、19D之2個或4個區 域，並以使各測溫體19所側定之測定值成為相等之方式， 师域_各歸加熱！！ 17進行開關㈣之溫度調整，而 藉此將模具本體10在預定溫度内保持為一定。在此，所謂 區域内的插裝加熱H ’當為4個區域時，是指接近於測: 體19之2個插裝加熱器17、π。 當將模具本體10分割為2個區域時，例如當位 卻水的上制mu 19B的測定溫度較減設定的預定 321055 19 溫度低時，係導通位於上游側之4個插裝加熱@ i7，成為 力熱狀,¾、來提间溫度。或者是當位於下游側之測溫體· 的别疋溫度較預先設定的預定溫度高時，係顏位於下游 側之4個插裝加熱盗17，解除加熱狀態來降低溫度。 藉由進行此溫度調整，可縮小在處理室4内因刀具3 的旋轉造成循環水的碰撞情形所導致之溫度差，使模具本 吐出面⑴中溫度成為一致，而能夠成形粒徑 更為均一之粒子。 於上述本實卿態之造粒用模具，造粒裝置，及發泡 性熱可塑性樹絲子的製造方法中，樹脂流路14及喷嘴 係在藉由插裝加熱器17從兩側夾持之狀態下被加熱。 所以不會僅加熱樹脂流路的單側，而能夠從兩側以等距離 均等地加熱’因此可抑制喷冑15白勺阻塞。結i可改善因阻 塞所導致之生產效率的降低，並製造出均—粒徑的高品質 敍早。 接下來根據圖面來說明本發明的實施形態之變形 例’關於與上述實施形態為相同或同等的構件或部分，係 2相同圖號並省略該說明’並說明與實施形態為不同之 構成。 的圖 第5圖為顯示本實施形態之變形例㈣嘴之配置狀態 ，為對應第4圖之圖。 5圖赫之變形例的樹脂流路i4A，其剖面形狀呈 ’於該梯形狀的範圍内設置有任意地配置了複數個 早體貝嘴心心……之噴嘴…形成樹脂流路⑽ 321055 20 #卜=廓之斜面14a、14b (直線部），係與插裝加熱器Η ，長度方向大致平行軌置而構成1本變形例中，由於 呈梯形狀的剖面之樹脂流路14A的斜面14a、咐相對於 插裝加熱器17成為等距離，所以可藉由插裝錢器以 增加均等加熱之面積，較圓形剖面的樹脂流路14更能夠均 等地加熱，因此可減少噴嘴的阻塞。 14無為了也明本貝施形態之造粒用模具’造粒裝置及發泡Polystyrene resin. Polystyrene resin, for example, styrene, α _ f styrene, vinyl toluene, chlorostyrene, ethyl styrene, isopropyl styrene, dimethyl styrene, styrene, etc. The individual polymer of the vinyl monomer or the copolymer of these is preferably a polystyrene resin which is preferably a polystyrene resin containing 50% by mass or more of styrene. Further, the polystyrene-based resin may be the styrene-based monomer containing the styrene monomer as a main component, and the styrene-based monomer 321055 16 1359068 '奚 ' ' a copolymer of a monomer such as (A.:) methyl acrylate, ethyl (meth) acrylate, (5) butyl acrylate, methyl hexaacetate, etc. (methyl) Acrylic acid-based vinegar; (methyl'-) acrylonitrile, cis-butanedicarboxylic acid dimethyl vinegar, anti-butadibilic acid dimethyl vinegar, anti-I-ene, acid diethyl vinegar, fumaric acid vinegar Further, for example, a difunctional monomer such as divinyl-methacrylic acid-extended diol vinegar or the like may be mentioned. In addition, as long as it is a polystyrene-based resin as a main component, it is possible to add another resin, and to increase the impact resistance of the foamed molded article, for example, polybutadiene, stupid ethylene, and dibutyl are added. A copolymer of a olefinic copolymer, an ethylene-propylene non-common vehicle, a dilute three-dimensional copolymer, and the like, and a rubber-like polymer, which is a so-called impact-resistant polystyrene. Alternatively, a polyethylene-based resin, a polypropylene-based resin, a propylene-glycolic acid-based resin, a acrylonitrile-styrene copolymer, an acrylonitrile-tau-di-b-ethyl-bond copolymer, or the like may be used. In the foamable thermoplastic resin particles of the present invention, polystyrene explosive resin is used as the foaming polystyrene resin resin granules of the thermoplastic resin, and the polystyrene resin as the raw material is excluded. A polyphenylene-based resin which is a non-recycled raw material such as a polystyrene resin which is newly produced by a method such as a suspension polymerization method, which is a commercially available general polystyrene-based resin (hereinafter referred to as non-repolymerization) It is also possible to use a recycled raw material obtained by regenerating a used polystyrene-based resin foam molded body in addition to benzene. For the recovered raw material, for example, the following recycled raw materials can be used, that is, the used polystyrene-based resin foam molded body can be recovered, for example, a fish tank, a household material, a cushioning material, a food package, and the like, and the lemon can be used. The recovered raw material is regenerated by the way of dissolving the oil or by heating and reducing the volume. In addition, it is possible to recover the raw material of 321055 .. 17 1359068, in addition to the remanufactured process of the used polystyrene-based resin foam molded body, there are also household appliances (such as televisions and electrics). A non-expanded polystyrene resin molded body separately recovered from a refrigerator, a washing machine, an air conditioner, or the like (for example, a photocopying machine, a facsimile machine, a printing machine, etc.) is pulverized and melt-kneaded to form a granular shape. Founder. As shown in Fig. 1 and Fig. 2, when the foaming thermoplastic resin particles are produced by using the granulator T, the thermoplastic resin is supplied from the supply hopper 21 to the granulation mold 1 at the tip end. The extruder 2 is melted and kneaded with the resin material. Next, while moving the thermoplastic resin toward the granule 1 for granulation, the foaming agent is pressed from the blowing agent supply port 22 to the thermoplastic resin by the high pressure pump 23, and the foaming agent is mixed with the thermoplastic resin. The resin 20 containing a foaming agent is formed. The resin 20 containing the foaming agent is transferred from the tip end of the extruder 2 to the resin flow path 14 of the mold main body 10 of the granulation mold 1 via the mold holder 11. The resin 20 containing the foaming agent conveyed by the resin flow path 14 is discharged from the respective nozzles 15 of the mold body 10, and is immediately immersed in the water flow (in the refrigerant) of the processing chamber 4 by the rotary blade of the cutter 2 Cut off. In the processing chamber 4, the resin 20 containing the foaming agent cut into a granular shape is a foamable thermoplastic resin particle having almost spherical shape. The foamable thermoplastic resin particles are transported in the line 5 with water, and reach the dehydration treatment unit 8, where the foamable thermoplastic resin particles are separated from the circulating water, dehydrated, dried, and separated. The water is sent to the sink 7. After the dehydration treatment unit 8 is separated and dehydrated and dried, the foaming 18 321055 1359068 thermoplastic resin particles 'is transferred to the container 9 and stored in the container. The foaming agent is not particularly limited, and for example, it may be separately It is used by using n-pentane, isoprene, cyclopentene, cyclopentadienyl or the like, or a mixture of two or more. Further, those in which the above pentanes are mainly used and n-butane, isobutylene or propylene are mixed may be used. In particular, it is preferable that the money is easy to suppress the foaming of the particles when ejected from the nozzle to the water flow. In addition, the foamable thermoplastic resin particles are those which contain a hair (4) in a thermoplastic resin and are formed into a pellet shape, and preferably have a small spherical shape. The foamable thermoplastic resin particles can be used for the following purposes, that is, heating in a free space to pre-expand, and the pre-expanded particles are injected into a mold having a desired function. In the inside of the hole, after the steam is added, the pre-existing mist is secreted, and then the mold is released to produce a foamed resin molded article having a desired shape. Next, a method of adjusting the temperature of the granule 丨 for granulation described above will be described. / As shown in Figure 3, in the granulation mold! In the temperature adjustment method, the mold main body 1G is divided into two or four regions corresponding to the upper and lower left and right temperature measuring bodies 19A, 19B, 19C, and 19D provided in the vicinity of the resin discharge surface η, so that the respective temperatures are measured. The measured values set by the body 19 are equal, and the divisions are heated by each! ! 17 The temperature adjustment of the switch (4) is performed, whereby the mold body 10 is kept constant for a predetermined temperature. Here, when the intervening heating H' in the region is four regions, it means that the two insertion heaters 17, π are close to the body 19. When the mold body 10 is divided into two regions, for example, when the measured temperature of the upper-made mu 19B of the water is lower than the predetermined temperature of the predetermined 321055 19, the four plug-in heating@i7 on the upstream side is turned on. Become a hot, 3⁄4, to bring the temperature. Alternatively, when the temperature of the temperature measuring body located on the downstream side is higher than a predetermined temperature set in advance, the four plugging heat sinks 17 on the downstream side of the system are released, and the heating state is released to lower the temperature. By performing this temperature adjustment, the temperature difference caused by the collision of the circulating water due to the rotation of the cutter 3 in the processing chamber 4 can be reduced, and the temperature in the discharge surface (1) of the mold can be made uniform, and the particle size can be more uniform. particle. In the above-described granulation mold, granulation apparatus, and foaming thermoplastic tree manufacturing method, the resin flow path 14 and the nozzle are held by the insertion heater 17 from both sides. It is heated in the state. Therefore, it is not possible to heat only one side of the resin flow path, and it is possible to uniformly heat from both sides at equal distances. Therefore, the clogging of the squirt 15 can be suppressed. The knot i can improve the production efficiency caused by the blockage and produce a high quality of the homo-particle size. In the following, a modified example of the embodiment of the present invention will be described with respect to the same or equivalent elements as those of the above-described embodiment, and the same reference numerals will be omitted, and the description will be omitted, and a configuration different from the embodiment will be described. Fig. 5 is a view showing a state in which the nozzle of the modification (4) of the present embodiment is placed, and corresponds to Fig. 4 . The resin flow path i4A of the modified example of FIG. 5 has a cross-sectional shape of a nozzle in which a plurality of early body-shaped beak cores are disposed in a range of the trapezoidal shape. The resin flow path is formed (10) 321055 20 # The slanting surfaces 14a and 14b (straight line portions) of the ribs are arranged in a substantially parallel direction with the insertion heater Η, and the slant surface 14a of the resin flow path 14A having a trapezoidal cross section is formed in the present modification. Since the crucible is equidistant with respect to the interposer heater 17, the area of the uniform heating can be increased by inserting the money insert, and the resin flow path 14 of the circular cross section can be heated more uniformly, so that the clogging of the nozzle can be reduced. 14In order to clarify the granulation mold of the Beishi form ‘granulation device and foaming

/、.'可塑性樹脂粒子的製造方法之效果，以下係說明實施 例0 、 (實施例） [實施例1] 1^例1中，將第2圖及第3圖所示之造粒用模具 乙條m.1圖所示之造粒裝置T，以製造出發泡性聚苯 埶„、子月曰粒子。惟僅使用測溫體19A，對全部的插裝加 …盗Η進行開關控制而進行造粒賴具]的溫度調整。 於口k 90mm (L/D=35)的單軸播壓機，將8個第2 =示的構造之造粒關具，亦即具有15個直徑Μ匪、 二Γ長度3.Gmm的噴嘴.之孔盤（噴嘴單元），配置於樹 、s於疮面的圓周上’於樹脂吐出面側，以從兩側夹持連 、嘴早元之各樹脂流路之方式，使8飾裝加熱器（直 ^ 横切前述圓周而放射狀地配置在加熱器深度（離 罟，曰吐出+面之距離’相當於第2圖的圖號L) 15mm的位 了1^材之桓具安裝於表面中央部，將預先以 淚同摻合機使微粉末滑石〇.3質量份均一地混合至聚苯乙 321055 21 1359068 烯樹脂（Toy〇 Polystyrene公司製、商品名稱「HRM1〇N」） 貝：!：份者，以每小時13〇kg的比例供應至擠壓機内， 將擠壓機内的最高溫度設定在220ΐ ’使樹脂熔融後，將 相對於樹脂100質量份為6質量份的戊烷（異戊烷/正戊烷 =20/80混合物），作為發泡劑於擠壓機中途予以壓入。 之後，於擠壓機中一邊捏合樹脂與發泡劑，一邊使擠 壓機前端部的樹脂溫度成為17(rc來進行冷卻，並通過^ 裝於擠壓機的前端且保持在280〇C之前述模具，擠壓至3〇 °C的冷卻水進行循環之處理室内，同時使在圓周方向具有 10片刀片的高速旋轉刀具密著於模具，以每分鐘33〇〇轉 進行切斷，進行脫水乾燥而製得球形的發泡性聚苯乙烯樹 脂粒子。此時之發泡性笨乙烯樹脂粒子的吐出量為 138kg/h。 於此實施例1中，可獲得擠壓開始的第1小時之對模 具的樹脂導入部之壓力為17.OMPa，乾燥後之1〇〇粒樹脂 的質量為0.0724g，模具的開孔率為80,2%之良好的結果。 擠壓開始的第48小時之對模具的樹脂導入部之壓力 為17.3MPa，100粒樹脂的質量為〇.〇741g，模具的開孔率 為78.4%，可確認出能夠安定地擠壓48小時以上。 對於擠壓第48小時所採集之發泡性苯乙烯樹脂极 子，係藉由後述的方法製作出容積發泡倍數50倍（容積密 度0.02g/cm3)的預發泡粒子，並使用此預發泡粒子來製得 發泡倍數50倍（密度〇,〇2g/cm3)的發泡成形體。以目視 來觀察所製得之發泡成形體，並評估預發泡粒子對成形模 32.1055 22 1359068 • 具之充填性。 • <模具的開孔率> " 開孔率（模具表面之吐出喷嘴的擠壓時開孔率）=開 孔數/模具的全部喷嘴數xlOO (%)。 吐出量（kg/h)=每1小時之以刀具所切出之全部發 泡性粒子的總質量 =開孔數X切出個數xl粒質量 =開孔數X刀具刀片數X刀具轉數xl粒質量。 ® 由於開孔數=吐出量（kg/h) /[刀具刀片數X刀具轉數 (rph ) xl粒質量（kg/個）]，所以開孔率可由下式算出。 開孔率（E)=開孔數/全部吐出喷嘴數xlOO (%) =[Q/ (NxRx60x (M/100) /1000) ]Ηχ100 (%) (式中，Q為吐出量（kg/h )，N為刀具刀片的片數， R為刀具轉數（rpm) ’ Μ為100粒質量（g)(從發泡性粒 子選出任意的100粒，並以最小刻度為O.OOOlg的電子天 |平所量測之值為100粒質量），Η為模具的全部喷嘴數） <開孔率的評估基準> 開孔率（Ε)係以下列基準進行評估（參照後述的第 1表）。 ◎ : 50%SE 〇：40%SE<50% Δ ： 30%^E<40% x ： E<30% <發泡成形體的製造> 23 . * 321055 1359068 將上述擠壓第48小時所製得之發泡性苯乙烯樹月〜 子，於20°C下放置1天。之後，相對於發泡性笨乙 粒子的100質量份，係添加硬脂酸鋅01質量份、經基硬 脂酸三酸甘油酯0.05質量份、硬脂酸單酸甘油酯0 〇5質 量份，進行混合並被覆於樹脂粒子後，投入至小型抵次式 預發泡機（内容積40L)，一邊攪拌一邊藉由吹入壓〇.〇5MPa (計示壓）的水蒸氣進行加熱，而製作出容積發泡倍數5〇 倍（容積密度0.02g/cm3)的預發泡粒子。 接著於23°C使所製得之預發泡粒子熟成後’使用安裝 了外形尺寸300x400x 100mm (厚度30mm)且於内部具有 厚度5mm ' l〇mm、25mm的中間區隔部之模具之自動成形 機（積水工機製作所製、ACE-3SP型），以下列條件進行 成形而製得發泡倍數50倍（密度0.02g/cm3)的發泡成形 成形條件（ACE-3SPQS-成形模式） 成形蒸氣壓0.08MPa (計示壓） 模具加熱3秒 一邊加熱（壓力設定）0.03MPa (計示壓） 另一邊加熱2秒 雙邊加熱12秒 水冷10秒 設定取出面壓〇.〇2MPa <預發泡粒子之模具充填性的評估基準> 以目視觀察上述發泡成形體，並藉由下列方式來評估 24 321055 1359068 ‘ 模具充填性。 ♦ • ◎:至厚度5mm的中間區隔部分為止均可飽滿地充 填 〇：雖然厚度5mm的中間區隔部分之充填尚可且確 認到過大發泡粒，但可形成中間區隔部 △:於厚度5mm的中間區隔部分觀察到因克填不良 所導致之粒子缺損，且未完全形成中間區隔部 X :厚度5mm的中間區隔部分之充填不良，完全未形 •成中間區隔部 <粒子100粒的合計質量〉 於發泡性聚苯乙烯樹脂粒子中，任意選出之粒子100 粒的合計質量較理想為0.02至0.09g的範圍。當超過0.09g 時，難以充填至成形模具的細部，可能使能夠成形之模具 僅限於單純形狀者。此外，當未滿0.02g時，粒子的生產 性可能較差。更理想的範圍為0.04至0.06g。在聚苯乙烯 | 樹脂以外的樹脂中，於上述範圍乘上樹脂的比重後之值， 為較理想之粒子100粒的合計質量之範圍。 <預發泡粒子之容積發泡倍數的測定方法> 使用漏斗使充分乾燥後的預發泡粒子自然落下至量 筒（例如500ml的容量）内後，敲打量筒的底並充填預發 泡粒子至預發泡粒子的容積成為一定為止。測定此時之預 發泡粒子的容積與質量並藉由下式所算出。容積為lml單 位來讀取，質量以最小刻度0.01 g的電子天平進行測定。 苯乙烯系樹脂的樹脂比重以1.0來計算，容積發泡倍數係 25 321055 1359068 於小數點以下第1位進行四捨五入。 容積發泡倍數（倍）=預發泡粒子的容積（ml) /預發 泡粒子的質量（g ) X樹脂比重 <發泡成形體之發泡倍數的測定方法> 從充分乾燥後的發泡成形體，切出測定用試驗片（例 如300x400x30mm )，測定此試驗片的尺寸及質量，根據所 測定出之尺寸算出試驗片的體積，並藉由下式所算出。苯 乙烯系樹脂的樹脂比重為1.0。 發泡倍數（倍）=試驗片體積（cm3) /試驗片質量（g) X樹脂比重 [實施例2] 於實施例2中，除了安裝了將實施例1所使用之模具 往喷嘴單元連通的樹脂流路予以擴張（增加剖面積），並將 每個喷嘴單元的噴嘴數從15個增加至25個之模具之外， 其他與實施例1相同，以吐出量138kg/h而製得球形的發 泡性苯乙烯樹脂粒子。 於此實施例2中，擠壓開始的第1小時之對模具的樹 脂導入部之壓力為14.OMPa，乾燥後之樹脂粒子100粒的 質量為0.0465g，模具的開孔率為75.0%，此為良好的結 果。 擠壓開始的第48小時之對模具的樹脂導入部之壓力 為14.0MPa，100粒樹脂的質量為0.0465g，模具的開孔率 為75.0%，可確認出能夠安定地擠壓48小時以上。 對於擠壓第48小時所採集之發泡性苯乙烯樹脂粒 26 321055 1359068 .子，係藉由與實施例1相同的方法製作出容積發泡倍數5〇 •倍（容積密度〇.〇2g/cm3)的預發泡粒子，並使用此預發泡 粒子來製得發泡倍數50倍（密度0.02g/cm3)的發泡成形 •體。以目視來觀察所製得之發泡成形體，並評估預發泡粒 子對成形模具之充填性。 [實施例3] 於貝％例3中，除了在實施例2所使用之模具中使用 模具溫度測定用感測器（第3圖所示之測溫體19當中配置 於上下位置之19B (流入側）與19A (流出側）的2個）， 並將區域分割為模具之循環水流入侧（下側，第2圖的圖 號4a側）的4個加熱器與循環水流出側（上侧，第2圖的 圖號4b⑷的4個加熱器之2分割來進行控制，並將模具 保持在wc之外，其他與實施例2相同，以吐出量 而製得球形的發泡性苯乙烯樹脂粒子。 於此實施例3中’播壓開始的第卜】、時之對模具的樹 .脂導入部之壓力為13.3MPa，乾燥後之樹脂粒子議粒的 質量為0.0425g，模具的開孔率為82 〇%，此為良好的結 果。 擠塵開始的第48小時之對模具的樹脂導入部之壓力 為n.3MPa，_粒樹脂的質量為〇 〇4祝，模具的開孔率 為82.0%，可確認出能夠安定地擠壓私小時以上。 對於擠疋第48小化所採集之發泡性苯乙稀樹脂粒 子，係藉由與實關〗相_方法製作出容積發泡倍數％ 倍（容積密度O.OW)的預發泡粒子，並使用此預發泡 321055 27 1359068 粒子來製得發泡倍數50倍（密度0.02g/cm3)的發泡成形 體。以目視來觀察所製得之發泡成形體，並評估預發泡粒 子對成形模具之充填性。 [實施例4] 於實施例4中，除了使用將實施例2所使用之模具的 加熱器深度從15mm變更為30mm之模具之外，其他與實 施例2相同，以吐出量138kg/h而製得球形的發泡性苯乙 烯樹脂粒子。 於此實施例4中，擠壓開始的第1小時之對模具的樹 脂導入部之壓力為16.IMPa，乾燥後之樹脂粒子100粒的 質量為0.0524g，模具的開孔率為66.5%，此為良好的結 果。 擠壓開始的第48小時之對模具的樹脂導入部之壓力 為16.8MPa，100粒樹脂的質量為0.058lg，模具的開孔率 為60.0%，可確認出能夠安定地擠壓48小時以上。 對於擠壓第48小時所採集之發泡性苯乙烯樹脂粒 子，係藉由與實施例1相同的方法製作出容積發泡倍數50 倍（容積密度〇.〇2g/cm3)的預發泡粒子，並使用此預發泡 粒子來製得發泡倍數50倍（密度0.02g/cm3)的發泡成形 體。以目視來觀察所製得之發泡成形體，並評估預發泡粒 子對成形模具之充填性。 [實施例5] 於實施例5中，除了使用將實施例2所使用之模具的 加熱器深度從15mm變更為45mm之模具之外，其他與實 28 321055 1359068 - 施例2相同，以吐出量138kg/h而製得球形的發泡性苯乙 • 稀樹脂粒子。 於此實施例5中，擠壓開始的第1小時之對模具的樹 脂導入部之壓力為16.9MPa，乾燥後之樹脂粒子100粒的 質量為0.0670g，模具的開孔率為52.0%，此為良好的結 果。 擠壓開始的第48小時之對模具的樹脂導入部之壓力 為18.1MPa，100粒樹脂的質量為0.0871g，模具的開孔率 Φ 為40.0%，可確認出能夠安定地擠壓48小時以上。 對於擠壓第48小時所採集之發泡性苯乙烯樹脂粒 子，係藉由與實施例1相同的方法製作出容積發泡倍數50 倍（容積密度〇.〇2g/cm3)的預發泡粒子，並使用此預發泡 粒子來製得發泡倍數50倍（密度0.02g/cm3)的發泡成形 體。.以目視來觀察所製得之發泡成形體，並評估預發泡粒 子對成形模具之充填性。 •[實施例6] 於實施例6中，除了僅使用異戊烷作為發泡劑之外， 其他與實施例2相同，以吐出量138kg/h而製得球形的發 泡性苯乙烯樹脂粒子。 於此實施例6中，擠壓開始的第1小時之對模具的樹 脂導入部之壓力為15.1MPa，乾燥後之樹脂粒子100粒的 質量為0.0458g，模具的開孔率為76.1%，此為良好的結 果。 擠壓開始的第48小時之對模具的樹脂導入部之壓力 29 321055 1359068 為15.0MPa，100粒樹脂的質量為〇 〇46〗g，模具的開孔率 為75.6% ’可確認出能夠安定地擠壓48小時以上。 對於擠壓第48小時所採集之發泡性聚苯乙烯樹脂粒 子，係藉由與實施例1相同的方法製作出容積發泡倍數5〇 倍（容積密度0.02g/cm3)的預發泡粒子，並使用此預發泡 粒子來製得發泡倍數5〇倍（密度Q G2g/em3)的發泡成形 體以目視來觀察所製得之發泡成形體，並評估預發泡粒 子對成形模具之充填性。 [比較例1] 第6A圖為比較例丨中所使用之模具之剖面圖，第6B 圖為顯示模具的樹脂吐出面之側視圖。 於比較例1中，除了改變為第6A圖及第6B圖所示 之一般所知的構造之模具2〇，亦即將16個具有15個直徑 0.6mm、段道部長度3 〇mm的喷嘴之喷嘴單元（圖號15) 配置於圓周上’且於樹脂吐出面13侧不具有插裝加熱器 (亦即僅配置短加熱器18)之模具之外，其他與實施例i 相同，以吐出量138kg/h而製得球形的發泡性苯乙烯樹脂 粒子。 於此比較例1中，擠壓開始的第丨小時之對模具的樹 月曰導入。卩之麼力為較高的21.7MPa， 1〇〇粒的質量為 0.1322g，模具的開孔率為22 〇%。 隨著時間的經過，確認到樹脂導入部的壓力上升，由 於在擠壓開始的第6小時到達模具的耐壓上限值 (25MPa)，因此於6小時停止播壓。 321055 30 1359068 • [比較例2] • 第7A圖為比較例2中所使用之模具之剖面圖，第7B 圖為顯示模具的樹脂吐出面之側視圖。 於比較例2中，除了改變為第7A圖及第7B圖所示 之構造的模具30，亦即於樹脂吐出面13側配置4個插裝 加熱器17、17、…（直徑12mm )，且於加熱器深度15mm 的位置，橫切排列噴嘴單元的圓周而配置為十字狀，並且 於表面中央部安裝有隔熱材16之模具之外，其他與實施例 # 1相同，以吐出量138kg/h而製得球形的發泡性苯乙烯樹 脂粒子。 於此比較例2中，撥壓開始的第1小時之對模具的樹 脂導入部之壓力為稍高的20.0MPa， 100粒的質量為 0.1030g，模具的開孔率為28.2%。 隨著時間的經過，確認到樹脂導入部的壓力上升，由 於在擠壓開始的第10小時到達模具的耐壓上限值 φ (25MPa)，因此於10小時停止擠壓。 [比較例3] 第8A圖為比較例3中所使用之模具之剖面圖，第8B : 圖為顯示模具的樹脂吐出面之側視圖。 '於比較例3中，除了改變為第8A圖及第8B圖所示 ，公知之構造的模具40，亦即不具有隔熱材，於模具設置油 . 的流路41，從模具上下41a、41a使高溫的油流入，並通 過中央的環狀流路往左右41b、41b流出並返回油加熱器之 構造之模具，並且藉由以油作為熱媒體之間接加熱將模具 31 3210*55 1359068 保持在280°C之外，其他與實施例1相同，以吐出量138kg/h 而製得球形的發泡性苯乙烯樹脂粒子。 於此比較例3中，擠壓開始的第1小時之對模具的樹 脂導入部之壓力為18.0MPa，100粒的質量為0.0907g，模 具的開孔率為32.0%。 擠壓開始的第48小時之對模具的樹脂導入部之壓力 為21.8MPa，100粒樹脂的質量為0.0994g，模具的開孔率 為 29.2%。 對於擠壓第48小時所採集之發泡性苯乙烯樹脂粒 子，係藉由與實施例1相同的方法製作出容積發泡倍數50 倍（容積密度〇.〇2g/cm3)的預發泡粒子，並使用此預發泡 粒子來製得發泡倍數50倍（密度0.02g/cm3)的發泡成形 體。以目視來觀察所製得之發泡成形體，並評估預發泡粒 子對成形模具之充填性。 上述實施例1至6以及比較例1至3的結果，係整理 於第1表中一同顯示。 32 321055 1359068 【第1表】The effect of the method for producing a plastic resin particle is as follows. Example 0 and (Example) [Example 1] In Example 1 , the granulation mold shown in Figs. 2 and 3 is used. The granulating device T shown in the figure m.1 is used to produce foamable polyphenylene hydrazine 、 and 子 曰 曰 particles. However, only the temperature measuring body 19A is used, and all the plugging and smashing are controlled by the switch. The temperature adjustment of the granulation sifter is carried out. In the single-axis weaving machine with a mouth of 90 mm (L/D=35), eight granulations of the structure of the second == are shown, that is, having 15 diameters.孔, Γ Γ 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. 3. In the way of the resin flow path, the 8 decorative heaters are arranged so as to be perpendicular to the circumference and radially arranged at the heater depth (distance from the 罟, 曰 discharge + surface 'equal to the figure L of Fig. 2) 15 mm The cookware of the 1^ material is installed in the center of the surface, and the micro-powder talc is mixed in advance with a tear-mixing machine. 3 parts by mass is uniformly mixed to the polystyrene 321055 21 1359068 olefin resin (Toy〇Polystyrene company, the product name "HRM1〇N") Bay:!: Part, supplied to the extruder at a rate of 13 〇kg per hour, set the maximum temperature in the extruder at 220 ΐ ' to melt the resin Thereafter, 6 parts by mass of pentane (isopentane/n-pentane = 20/80 mixture) with respect to 100 parts by mass of the resin was pressed as a foaming agent in the middle of the extruder. Thereafter, in an extruder While the resin and the foaming agent were kneaded, the resin temperature at the front end portion of the extruder was cooled by 17 (rc), and the mold was placed at the front end of the extruder and held at 280 ° C, and pressed. The cooling water of 3 ° C is circulated in the treatment chamber, and a high-speed rotary cutter having 10 blades in the circumferential direction is adhered to the mold, and is cut at 33 rpm, and dehydrated and dried to obtain a spherical shape. Foaming polystyrene resin particles. The amount of foaming of the foamed vinyl resin particles at this time was 138 kg/h. In the first embodiment, the resin introduction portion of the mold for the first hour after the start of extrusion was obtained. The pressure is 17.OMPa, and 1 granule after drying The mass of the resin was 0.0724 g, and the opening ratio of the mold was good at 80% and 2%. The pressure at the resin introduction portion of the mold at the 48th hour from the start of extrusion was 17.3 MPa, and the mass of the 100 resin was 〇. 〇741g, the opening ratio of the mold was 78.4%, and it was confirmed that it can be stably pressed for 48 hours or more. The foamable styrene resin pole collected at the 48th hour of extrusion was produced by the method described later. A pre-expanded particle having a volume expansion ratio of 50 times (bulk density: 0.02 g/cm3) was used, and a foamed molded article having a foaming ratio of 50 times (density 〇, 〇2 g/cm3) was obtained using the pre-expanded particles. The obtained foamed molded body was visually observed, and the pre-expanded particles were evaluated for the filling property of the forming mold 32.1055 22 1359068. • <opening ratio of the mold>" opening ratio (opening ratio at the time of extrusion of the discharge nozzle of the mold surface) = number of openings / total number of nozzles of the mold x100 (%). Discharge amount (kg/h) = total mass of all foaming particles cut by the cutter per hour = number of openings X number of cuts xl grain mass = number of holes X number of tool blades X number of tool revolutions Xl grain quality. ® The opening ratio is calculated by the following formula because the number of openings = the amount of discharge (kg/h) / [number of tool inserts × number of tool revolutions (rph) x l mass (kg / piece)]. Opening ratio (E) = number of openings / number of all nozzles xlOO (%) = [Q / (NxRx60x (M/100) / 1000) ] Ηχ 100 (%) (where Q is the amount of discharge (kg/h) N, N is the number of cutter blades, R is the number of revolutions of the tool (rpm) 'Μ is 100 pellets (g) (select 100 particles from the foaming particles, and the electronic scale with the minimum scale of O.Onglg The value measured by the flat is 100 masses), and the number of all the nozzles of the mold is as follows. <Evaluation criteria of the opening ratio> The opening ratio (Ε) is evaluated by the following criteria (refer to the first table described later). ). ◎ : 50% SE 〇: 40% SE < 50% Δ : 30% ^ E < 40% x : E < 30% < Manufacture of foamed molded article > 23 . * 321055 1359068 The above-mentioned pressing 48 hours The foamed styrene tree obtained was placed at 20 ° C for 1 day. Then, 01 parts by mass of zinc stearate, 0.05 parts by mass of stearic acid triglyceride, and 5 parts by mass of stearic acid monoglyceride are added to 100 parts by mass of the foamable ethyl bromide particles. After being mixed and coated with the resin particles, the mixture is placed in a small-sized pre-expander (40 L of internal volume), and heated by steaming with a pressure of 5 MPa (measured by pressure) while stirring. Pre-expanded particles having a volume expansion ratio of 5 〇 (bulk density: 0.02 g/cm 3 ) were produced. Then, after the pre-expanded particles obtained were cooked at 23 ° C, the automatic molding of a mold having an outer dimension of 300 mm × 400 × 100 mm (thickness: 30 mm) and having a thickness of 5 mm 'l〇mm, 25 mm inside was used. Machine (manufactured by Sekisui Seisakusho Co., Ltd., ACE-3SP type), which was molded under the following conditions to obtain a foam molding molding condition (ACE-3SPQS-forming mode) with a foaming multiple of 50 times (density 0.02 g/cm3). Pressure 0.08MPa (measured pressure) The mold is heated for 3 seconds while heating (pressure setting) 0.03MPa (measured pressure) The other side is heated for 2 seconds, bilateral heating for 12 seconds, water cooling for 10 seconds, setting of the extraction surface pressure 〇. 〇 2MPa < pre-expansion Evaluation criteria of mold filling property of particles> The above-mentioned foamed molded body was visually observed, and 24 321055 1359068 'mold filling property was evaluated by the following method. ♦ • ◎: The intermediate section can be filled to a thickness of 5 mm. Although the intermediate section of the thickness of 5 mm is filled and the oversized foaming particles are confirmed, the intermediate partition can be formed. The intermediate portion of the thickness of 5 mm was observed to have a particle defect caused by poor filling, and the intermediate portion X was not completely formed: the filling of the intermediate portion having a thickness of 5 mm was completely unshaped, and the intermediate portion was completely formed. In the foamable polystyrene resin particles, the total mass of 100 particles selected arbitrarily is preferably in the range of 0.02 to 0.09 g. When it exceeds 0.09 g, it is difficult to fill the details of the molding die, and it is possible to make the mold that can be formed limited to a simple shape. In addition, when less than 0.02 g, the productivity of the particles may be poor. A more desirable range is from 0.04 to 0.06 g. In the resin other than the polystyrene resin, the value obtained by multiplying the specific gravity of the resin in the above range is a range of the total mass of 100 particles of the preferred particles. <Method for Measuring Volume Expansion Ratio of Pre-expanded Particles> After the sufficiently dried pre-expanded particles are naturally dropped into a measuring cylinder (for example, a capacity of 500 ml) using a funnel, the bottom of the measuring cylinder is tapped and the pre-expanded particles are filled. The volume until the pre-expanded particles is constant. The volume and mass of the pre-expanded particles at this time were measured and calculated by the following formula. The volume is read in units of 1 ml and the mass is measured with an electronic balance with a minimum scale of 0.01 g. The specific gravity of the resin of the styrene resin is 1.0, and the volume expansion ratio is 25 321055 1359068 rounded off to the first place below the decimal point. Volume expansion ratio (times) = volume of pre-expanded particles (ml) / mass of pre-expanded particles (g) X resin specific gravity <Method for measuring foaming ratio of foamed molded article> The foamed molded article was cut out, and a test piece for measurement (for example, 300×400×30 mm) was cut out, and the size and mass of the test piece were measured, and the volume of the test piece was calculated from the measured size, and was calculated by the following formula. The specific gravity of the styrene resin is 1.0. Expansion ratio (times) = test piece volume (cm3) / test piece quality (g) X resin specific gravity [Example 2] In Example 2, except that the mold used in Example 1 was attached to the nozzle unit The resin flow path was expanded (increased sectional area), and the number of nozzles per nozzle unit was increased from 15 to 25, and the same as in Example 1, the spherical amount was obtained by discharging 138 kg/h. Expandable styrene resin particles. In the second embodiment, the pressure of the resin introduction portion of the mold in the first hour after the start of extrusion was 14.0 MPa, the mass of 100 particles of the resin particles after drying was 0.0465 g, and the opening ratio of the mold was 75.0%. This is a good result. The pressure at the resin introduction portion of the mold at the 48th hour after the start of extrusion was 14.0 MPa, the mass of 100 pellets was 0.0465 g, and the opening ratio of the mold was 75.0%, and it was confirmed that the pressure was stably pressed for 48 hours or longer. For the foaming styrene resin pellets 26 321055 1359068 obtained at the 48th hour of extrusion, a volume expansion ratio of 5 〇•倍 was produced by the same method as in Example 1 (volume density 〇.〇2g/ The pre-expanded particles of cm3) were used, and the pre-expanded particles were used to obtain a foamed molded body having a foaming ratio of 50 times (density of 0.02 g/cm3). The obtained foamed molded body was visually observed, and the filling property of the pre-expanded particles to the forming mold was evaluated. [Example 3] In Example 3, in Example 3, a mold temperature measuring sensor was used in the mold used in Example 2 (19B placed in the upper and lower positions among the temperature measuring bodies 19 shown in Fig. 3 (inflow) (the side) and the 19A (outflow side), and the area is divided into four heaters on the circulating water inflow side of the mold (lower side, the figure 4a side of Fig. 2) and the circulating water outflow side (upper side) The four heaters of Fig. 4b (4) in Fig. 2 are divided into two, and the mold is held outside the wc. Similarly, in the same manner as in the second embodiment, a spherical expandable styrene resin is obtained by the discharge amount. In the third embodiment, the 'division of the start of the weaving pressure】, the time of the tree to the mold, the pressure of the fat introduction portion is 13.3 MPa, and the mass of the resin particles after drying is 0.0425 g, and the opening of the mold The rate is 82%, which is a good result. The pressure at the resin introduction portion of the mold at the 48th hour of the start of the dust is n.3 MPa, the mass of the granule resin is 〇〇4, and the opening ratio of the mold is 82.0%, it can be confirmed that it can be squeezed stably for more than a few hours. The styrene styrene resin particles are pre-expanded particles having a volume expansion ratio of doubling times (volume density O.OW) by using the method of real-time crystallization, and using the pre-expanded 321055 27 1359068 particles. A foamed molded article having a foaming ratio of 50 times (density: 0.02 g/cm 3 ) was obtained. The obtained foamed molded article was visually observed, and the filling property of the pre-expanded particles to the forming mold was evaluated. [Example 4] In the fourth embodiment, in the same manner as in the example 2 except that the depth of the heater of the mold used in the second embodiment was changed from 15 mm to 30 mm, spherical foaming was obtained at a discharge amount of 138 kg/h. The styrene resin particles. In the fourth embodiment, the pressure of the resin introduction portion of the mold at the first hour of the extrusion was 16.IMPa, and the mass of the resin particles after drying was 0.0524 g, and the mold was opened. The porosity was 66.5%, which was a good result. The pressure at the resin introduction portion of the mold at the 48th hour from the start of the extrusion was 16.8 MPa, the mass of the 100 resin was 0.058 lg, and the opening ratio of the mold was 60.0%. It can be confirmed that it can be stably pressed for more than 48 hours. For the foamable styrene resin particles collected in 48 hours, pre-expanded particles having a volume expansion ratio of 50 times (volume density 〇.〇2 g/cm 3 ) were produced by the same method as in Example 1, and used. The foamed molded body having a foaming ratio of 50 times (density: 0.02 g/cm 3 ) was obtained by pre-expanding the particles. The obtained foamed molded body was visually observed, and the filling property of the pre-expanded particles to the forming mold was evaluated. [Example 5] In Example 5, except that the mold having the depth of the mold used in Example 2 was changed from 15 mm to 45 mm, the same as that of the actual 28 321055 1359068 - Example 2, to spit out The spherical foamable styrene resin particles were obtained in an amount of 138 kg/h. In the fifth embodiment, the pressure at the resin introduction portion of the mold at the first hour after the start of extrusion was 16.9 MPa, the mass of the resin particles 100 after drying was 0.0670 g, and the opening ratio of the mold was 52.0%. For good results. The pressure at the resin introduction portion of the mold at the 48th hour after the start of extrusion was 18.1 MPa, the mass of 100 pellets was 0.0871 g, and the opening ratio Φ of the mold was 40.0%, and it was confirmed that the mold was stably pressed for 48 hours or more. . For the expandable styrene resin particles collected at the 48th hour of extrusion, pre-expanded particles having a volume expansion ratio of 50 times (volume density 〇.〇2g/cm3) were produced by the same method as in Example 1. Using this pre-expanded particle, a foamed molded article having a foaming ratio of 50 times (density of 0.02 g/cm3) was obtained. The obtained foamed molded body was visually observed, and the filling property of the pre-expanded particles to the forming mold was evaluated. [Example 6] In the same manner as in Example 2 except that only isopentane was used as the foaming agent, spherical foamable styrene resin particles were obtained at a discharge amount of 138 kg/h. . In the sixth embodiment, the pressure of the resin introduction portion of the mold at the first hour after the start of extrusion was 15.1 MPa, and the mass of the resin particles 100 after drying was 0.0458 g, and the opening ratio of the mold was 76.1%. For good results. At the 48th hour from the start of extrusion, the pressure of the resin introduction portion of the mold was 29 321055 1359068, which was 15.0 MPa, the mass of 100 resin was 〇〇46〗, and the opening ratio of the mold was 75.6%. Squeeze for more than 48 hours. For the expandable polystyrene resin particles collected at the 48th hour of extrusion, pre-expanded particles having a volume expansion ratio of 5 〇 (bulk density: 0.02 g/cm 3 ) were produced in the same manner as in Example 1. And using the pre-expanded particles to obtain a foam molded body having a foaming ratio of 5 〇 (density Q G2g/em3), visually observing the obtained foamed molded body, and evaluating the pre-expanded particle pair forming Filling of the mold. [Comparative Example 1] Fig. 6A is a cross-sectional view of a mold used in a comparative example, and Fig. 6B is a side view showing a resin discharge surface of a mold. In Comparative Example 1, except for the mold 2 which was changed to the generally known structure shown in Figs. 6A and 6B, 16 nozzles having 15 diameters of 0.6 mm and a section length of 3 mm were used. The nozzle unit (FIG. 15) is disposed on the circumference and has no mold for inserting the heater on the resin discharge surface 13 side (that is, the short heater 18 is disposed only), and the discharge amount is the same as that of the embodiment i. Spherical expandable styrene resin particles were obtained at 138 kg/h. In Comparative Example 1, the 丨 hour of the start of the extrusion was introduced into the mold of the mold. The force of the crucible is 21.7 MPa, the mass of the 1 granule is 0.1322 g, and the opening ratio of the mold is 22 〇%. As time passed, it was confirmed that the pressure of the resin introduction portion was increased, and the pressure resistance upper limit (25 MPa) of the mold was reached at the sixth hour from the start of the extrusion, so that the pressure was stopped at 6 hours. 321055 30 1359068 • [Comparative Example 2] Fig. 7A is a cross-sectional view of a mold used in Comparative Example 2, and Fig. 7B is a side view showing a resin discharge surface of the mold. In Comparative Example 2, in addition to the mold 30 having the structure shown in FIGS. 7A and 7B, four cartridge heaters 17, 17, ... (diameter 12 mm) are disposed on the resin discharge surface 13 side, and At a position where the depth of the heater was 15 mm, the circumference of the nozzle unit was arranged to be cross-shaped, and the mold was placed in the center of the surface, and the same as in Example #1, the discharge amount was 138 kg/ h A spherical expandable styrene resin particle was obtained. In Comparative Example 2, the pressure of the resin introduction portion of the mold at the first hour from the start of the pressing was slightly higher at 20.0 MPa, the mass of 100 particles was 0.1030 g, and the opening ratio of the mold was 28.2%. As time passed, it was confirmed that the pressure of the resin introduction portion was increased, and since the pressure-resistant upper limit value φ (25 MPa) of the mold reached the 10th hour after the start of extrusion, the extrusion was stopped for 10 hours. [Comparative Example 3] Fig. 8A is a cross-sectional view of a mold used in Comparative Example 3, and Fig. 8B is a side view showing a resin discharge surface of the mold. In Comparative Example 3, except for the change to the 8A and 8B drawings, the mold 40 of the known structure, that is, the heat insulating material is not provided, and the flow path 41 of the oil is provided in the mold, from the upper and lower 41a of the mold. 41a allows the high-temperature oil to flow in, and flows through the central annular flow path to the left and right 41b, 41b and returns to the mold of the oil heater, and the mold 31 3210*55 1359068 is maintained by heating the oil as a heat medium. In the same manner as in Example 1 except for 280 ° C, spherical foamable styrene resin particles were obtained at a discharge amount of 138 kg/h. In Comparative Example 3, the pressure at the resin introduction portion of the mold at the first hour after the start of extrusion was 18.0 MPa, the mass of 100 pellets was 0.0907 g, and the opening ratio of the mold was 32.0%. The pressure at the resin introduction portion of the mold at the 48th hour from the start of extrusion was 21.8 MPa, the mass of 100 pellets was 0.0994 g, and the opening ratio of the mold was 29.2%. For the expandable styrene resin particles collected at the 48th hour of extrusion, pre-expanded particles having a volume expansion ratio of 50 times (volume density 〇.〇2g/cm3) were produced by the same method as in Example 1. Using this pre-expanded particle, a foamed molded article having a foaming ratio of 50 times (density of 0.02 g/cm3) was obtained. The obtained foamed molded body was visually observed, and the filling property of the pre-expanded particles to the forming mold was evaluated. The results of the above Examples 1 to 6 and Comparative Examples 1 to 3 are shown together in the first table. 32 321055 1359068 [Table 1]

m I S 丨 疙< ^途 ,00 s§^ 1 32.0 (77 孔） Δ 1 Ssx 阳x g o X cs 1 •u _ S赶 ，g VO S§® 1 Φ 穹 Μη Ιΐί 1 1 1 1 s •u ηδΐϊτ 雖 g Ό S討 χ III v〇 s^cQ 11¾ 1 1 1 v〇 I ϊ^ι IS沄杯 g s VO SI® jn gg© VD^n JQ2® T-H 1 C> ◎ in ¥ 加熱器 深度 45mm VO SI另 ON vd §s@ 〇〇 l!〇 TO § 〇 寸 I ixiraoe 系游 MW碎 ί-Η VO SI® \D 3?® rn oo 1r@ 00 s o ◎ m I 上下分割溫 度調整 (測溫感測 器2個） 加熱器深度 15mm VO Si® m r〇 r—4 IS® cn rn i '"i §s@ § s o ◎ CN I f睽！ §苫沄杷 § VO s轉 o §δ@ | idg© m 1 〇· ◎ .τ·Η ψί 5¾^ | }鲢！ KO ss® g φ rn T-H | 〇 #wiy (画）獅象鄉 (ΠΠΠ)香剛4 (卧）潘祕 I aW 3Ϊ i § 1 $ PP^ as eM Ifl g蹇鸯 /-N I f| s鹚 lit Hub 蛛5 [第48小時j 模具壓力（MPa) ( -¾ §5 n- Πΰ? 〇£ 3 φΗ ^S wl If ^ II 33 321055 1359068 從第1表的結果中可得知，於本發明之實施例1至6 中，從造粒開始的第1小時之模具壓力為13.3至 17.0MPa，第48小時之模具壓力為13.3至18.1MPa，均較 比較例1至3低，因此可連續進行運轉。此外，模具的開 孔率在經過1小時的時候均為52%以上，經過48小時的 時候均為40%以上，尤其是實施例1至3以及實施例6中， 經過1小時的時候均為75%以上，經過48小時的時候均 為75%以上，可確認出開孔率（E)隨著時間的經過幾乎 不會改變。 此外，於加熱器深度45mm的實施例5中，開孔率較 加熱器深度3 0mm的實施例4為降低，因此，加熱器深度 較理想為10至50mm，更理想為15至30mm。 另一方面，於比較例1、2中，可顯著觀察到因喷嘴 阻塞所導致之模具壓力的上升，於6至10小時左右的運轉 下，即已到達模具耐壓上限。模具的開孔率在經過1小時 的時候，已到達22.0至32.0%之低比例。 比較例3，相較於實施例1至6，就於模具内設置環 狀油流路者，會導致模具構造變得複雜，且必須準備油的 加熱器及循環泵浦，以及須對使油循環之配管進行保溫 等，導致設置成本的提高。此外，亦具有因劣化的油或雜 質導致流路的阻塞，變得不易流動而使加熱均衡性喪失， 而無法均一地保持模具溫度等缺點。 以上係說明本發明之造粒用模具，造粒裝置及發泡性 熱可塑性樹脂粒子的製造方法之實施形態，但本發明並不 34 321055 1359068 限定於上述實施形態，在不脫離該主旨之範圍内，可適當 • 地進行變更。 〜 例如，於本實施形態中，樹脂流路14係設定有8處， 且插裝加熱器17及短加熱器18分別具有8個，但並不限 定於此數量，可因應造粒用模具1的大小、熱可塑性樹脂 粒子的成形量等條件，來設定為最適的數量。總而言之， 只要是在樹脂流路14之圓周的周方向兩側配置有插裝加 熱器17之構成者即可。 I 此外，測溫體19係設定為4個，但並不限定於此， 例如測溫體19可為位於上下位置的2個。 再者，關於擠壓機2、刀具3、處理室4、模具固持器 11、模具本體10等的形狀、大小及其他構成，並無特別限 制，可任意地設定。例如，於本實施形態中，樹脂供應裝 置係採用擠壓機，但除此之外，亦可使用靜態摻合機、齒 輪泵浦等。 P [產業利用可能性] 根據本發明，係提供可防止於依據熱切法之造粒用模 具中之喷嘴的阻塞，而能夠有效率地生產出均一粒徑的粒 子之造粒用模具，造粒裝置及發泡性熱可塑性樹脂粒子的 製造方法。 【圖式簡單說明】 第1圖為本發明實施形態之造粒裝置之構成圖。 第2圖為顯示本發明實施形態之造粒用模具的概略構 成之側視剖面圖。 35 321055 第3圖為顯示第2圖之模具本體的樹脂吐出面之側視 第4圖為顯示噴嘴之配置狀態的一例圖。 第5圖為顯示本實施形態之變形例的噴嘴之配置狀態 的一例圖’為對應第4圖之圖。 第6Α圖為比較例1中所使用之模具之剖面圖。 第6Β圖為顯示比較例1中所使用之模具的樹脂吐出 面之側視圖。 第7Α圖為比較例2中所使用之模具之剖面圖。 第7Β圖為顯示比較例2中所使用之模具的樹脂吐出 面之側視圖。 第8Α圖為比較例3中所使用之模具之剖面圖。 第8Β圖為顯示比較例3中所使用之模具的樹脂吐出 面之側視圖。 【主要元件符號說明】 1 造粒用模具 2 擠壓機（樹脂供應裝置） 3 刀具 4 處理室 4a 循環水流入侧 4b 循環水流出側 5 管路 6 送水泵浦 10 模具本體 36 321055m IS 丨疙< ^ way, 00 s§^ 1 32.0 (77 holes) Δ 1 Ssx yang xgo X cs 1 •u _ S catch, g VO S§® 1 Φ 穹Μη Ιΐί 1 1 1 1 s •u Ηδΐϊτ Although g Ό S Discussion III v〇s^cQ 113⁄4 1 1 1 v〇I ϊ^ι IS沄 Cup gs VO SI® jn gg© VD^n JQ2® TH 1 C> ◎ in ¥ Heater depth 45mm VO SI another ON vd §s@ 〇〇l!〇TO § I I ixiraoe 游 MW ί Η VO VO SI® \D 3?® rn oo 1r@ 00 so ◎ m I up and down split temperature adjustment (temperature sense 2 detectors) Heater depth 15mm VO Si® mr〇r—4 IS® cn rn i '"i §s@ § so ◎ CN I f睽! §苫沄杷§§ VO s turn o §δ@ | idg© m 1 〇· ◎ .τ·Η ψί 53⁄4^ | }鲢! KO ss® g φ rn TH | 〇#wiy (画) 狮象乡(ΠΠΠ)香刚4 (卧)潘秘 I aW 3Ϊ i § 1 $ PP^ as eM Ifl g蹇鸯/-NI f| s鹚Lit Hub Spider 5 [48th hour j mold pressure (MPa) ( -3⁄4 §5 n- Πΰ? 3£ 3 φΗ ^S wl If ^ II 33 321055 1359068 It can be seen from the results of Table 1 that the present invention In Examples 1 to 6, the mold pressure at the first hour from the granulation was 13.3 to 17.0 MPa, and the mold pressure at the 48th hour was 13.3 to 18.1 MPa, which were lower than those of Comparative Examples 1 to 3, so that continuous operation was possible. In addition, the opening ratio of the mold was 52% or more after 1 hour, and 40% or more after 48 hours, especially in Examples 1 to 3 and Example 6, after 1 hour. Both were 75% or more, and when it was 48 hours or more, it was 75% or more, and it was confirmed that the opening ratio (E) hardly changed with time. Further, in Example 5 in which the heater depth was 45 mm, it was opened. The porosity of Example 4 is lower than that of the heater depth of 30 mm, and therefore, the heater depth is desirably 10 to 50 mm, more preferably 15 to 30 mm. In Examples 1 and 2, the increase in mold pressure due to nozzle clogging was observed significantly, and the operation reached the upper limit of the mold under the operation of about 6 to 10 hours. The opening ratio of the mold was 1 hour. , has reached a low ratio of 22.0 to 32.0%. In Comparative Example 3, the arrangement of the annular oil flow path in the mold compared to Examples 1 to 6 causes the mold structure to be complicated, and the oil heating must be prepared. And the pumping of the oil, as well as the need to keep the piping for the oil circulation, etc., resulting in an increase in the installation cost. In addition, there is a blockage of the flow path due to degraded oil or impurities, which makes it difficult to flow and loses the heating balance. However, the above-described embodiments of the granulation mold, the granulation apparatus, and the method for producing the foamable thermoplastic resin particles of the present invention are described. However, the present invention is not limited to 34 321055 1359068. The above-described embodiment can be appropriately changed without departing from the scope of the invention. 〜 For example, in the present embodiment, the resin flow path 14 is set in eight places, and the insertion and addition are performed. The number of the ejector 17 and the short heaters 18 is eight, but the number is not limited thereto, and the optimum amount can be set in accordance with conditions such as the size of the granule 1 for granulation and the amount of molding of the thermoplastic resin particles. It is sufficient that the plug-in heater 17 is disposed on both sides of the circumferential direction of the circumference of the resin flow path 14. I Further, the temperature measuring body 19 is set to four, but is not limited thereto, and for example, a temperature measuring body 19 can be two located at the upper and lower positions. Further, the shape, size, and other configurations of the extruder 2, the cutter 3, the processing chamber 4, the mold holder 11, the mold body 10, and the like are not particularly limited, and can be arbitrarily set. For example, in the present embodiment, the resin supply device is an extruder, but in addition to this, a static blender, a gear pump, or the like may be used. P [Industrial Applicability] According to the present invention, there is provided a granulation mold which can prevent the clogging of nozzles in a granulation mold according to the hot cutting method, and can efficiently produce particles having a uniform particle size, and granulate A method for producing a device and foamable thermoplastic resin particles. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a configuration diagram of a granulation apparatus according to an embodiment of the present invention. Fig. 2 is a side sectional view showing a schematic configuration of a granulating mold according to an embodiment of the present invention. 35 321055 Fig. 3 is a side view showing the resin discharge surface of the mold main body of Fig. 2. Fig. 4 is a view showing an example of the arrangement state of the nozzles. Fig. 5 is a view showing an example of an arrangement state of nozzles according to a modification of the embodiment, and Fig. 4 is a view corresponding to Fig. 4. Fig. 6 is a cross-sectional view of the mold used in Comparative Example 1. Fig. 6 is a side view showing the resin discharge surface of the mold used in Comparative Example 1. Fig. 7 is a cross-sectional view of the mold used in Comparative Example 2. Fig. 7 is a side view showing the resin discharge surface of the mold used in Comparative Example 2. Fig. 8 is a cross-sectional view of the mold used in Comparative Example 3. Fig. 8 is a side view showing the resin discharge surface of the mold used in Comparative Example 3. [Description of main component symbols] 1 Pelletizing die 2 Extruder (resin supply device) 3 Tool 4 Processing chamber 4a Circulating water inflow side 4b Circulating water outflow side 5 Pipeline 6 Water pump 10 Mold body 36 321055

Claims (1)

•第9810^224號專利申請案 100年10月26日修正替換頁 1359068 ----| 咏私月絝(夫&gt;正替換衷系 . «. i “》·&gt;· -^ «»*» , · -· · 七、.申請寻利範圍：:;:： 1.二種造粒用模裏「其特徵為具備： 接觸於冷媒而設置之樹脂吐出面； 連通至樹脂供應裝置之複數個樹脂流路； 與前述樹脂流路連通且於前述樹脂吐出面形成開 口之喷嘴；以及 設置於前述樹脂吐出面的附近之複數個插裝加熱 口•口- · 益， 前述樹脂流路係沿著前述樹脂吐出面上之虛擬圓 鲁 的圓周而配置； 前述插裝加熱器係配置於前述複數個樹脂流路各 者之前述圓周的周方向兩側，並且以使長度方向朝向 前述圓周的徑方向且橫切前述圓周之狀態而配置。 2. 如申請專利範圍第1項之造粒用模具，其中，前述插 裝加熱器係設置8個以上； 各個插裝加熱器的中心角為45°以下。 φ 3. 如申請專利範圍第1項之造粒用模具，其中，前述插 裝加熱器係設置於距離前述樹脂吐出面為10至50mm 的位置。 4. 如申請專利範圍第1項之造粒用模具，其中，前述樹 脂流路的剖面形狀係於其外輪廓具有直線部； 前述直線部與前述插裝加熱器的長度方向大致平 行而配置。 5. 如申請專利範圍第1項之造粒用模具，其中，係於前 38 321055修正版 1359068 第98105224號專利申請案 100年10月26日修正替換頁 述樹脂流路沿著該前述剖面形狀設置有複數個喷嘴。 6. 如申請專利範圍第1項之造粒用模具，其中，至少於 前述冷媒之水流方向的上游側與下游側設置溫度感測 · 且構成為根據前述溫度感測器的測定溫度，個別 對前述插裝加熱器進行開關控制。 7. 一種造粒裝置，其特徵為具備： 申請專利範圍第1至6項中任一項之造粒用模具； • 將前述造粒用模具安裝於前端之樹脂供應裝置； 以及 收納有將從前述造粒用模具的喷嘴所吐出之樹脂 予以切斷之刀具，並且使冷媒與前述造粒用模具的樹 脂吐出面接觸之處理室。 8. 一種發泡性熱可塑性樹脂粒子的製造方法，其特徵為 具有： φ 將熱可塑性樹脂供應至安裝了申請專利範圍第1 至6項中任一項之造粒用模具之樹脂供應裝置，並進 行熔融捏合之步驟； 一邊使前述熱可塑性樹脂朝向前述造粒用模具移 動，一邊將發泡劑注入至前述熱可塑性樹脂以形成含 有發泡劑的樹脂之步驟；以及 藉由刀具，於冷媒中將從前述造粒用模具的喷嘴 所吐出之前述含有發泡劑的樹脂予以切斷，而製得發 泡性熱可塑性樹脂粒子之步驟。 39 321055修正版 1359068 •第9810；5224號專利申請案 100年10月26日修正替換頁 9. 如申請專利範圍第8項之發泡性熱可塑性樹脂粒子的 製造方法，其中，係至少測定冷媒之水流方向的上游 侧與下游侧之模具溫度，並且以使各個測定值成為相 等之方式，個別對各Μ裝加熱器進行開關控制。 10. —種熱可塑性樹脂發泡粒子的製造方法，其特徵為具 有： 將熱可塑性樹脂供應至安裝了申請專利範圍第1 至6項中任一項之造粒用模具之樹脂供應裝置，並進 行熔融捏合之步驟； β 一邊使前述熱可塑性樹脂朝向前述造粒用模具移 動，一邊將發泡劑注入至前述熱可塑性樹脂以形成含 有發泡劑的樹脂之步驟； 藉由刀具，於冷媒中將從前述造粒用模具的喷嘴 所吐出之前述含有發泡劑的樹脂予以切斷，而製得發 泡性熱可塑性樹脂粒子之步驟；以及 使前述發泡性熱可塑性樹脂粒子預發泡，而製得 0 熱可塑性樹脂發泡粒子。 11. 一種熱可塑性樹脂發泡成形體的製造方法，其特徵為 具有： 將熱可塑性樹脂供應至安裝了申請專利範圍第1 至6項中任一項之造粒用模具之樹脂供應裝置，並進 行熔融捏合之步驟； 一邊使前述熱可塑性樹脂朝向前述造粒用模具移 動，一邊將發泡劑注入至前述熱可塑性樹脂以形成含 40 321055修正版 1359068 _ 第98105224號專利申請案 • 100年10月26日修正替換頁 有發泡劑的樹脂之步驟； 藉由刀具，於冷媒中將從前述造粒用模具的喷嘴 所吐出之前述含有發泡劑的樹脂予以切斷，而製得發 - 泡性熱可塑性樹脂粒子之步驟； 加熱前述發泡性熱可塑性樹脂粒子使其預發泡， 而製得熱可塑性樹脂發泡粒子；以及 使前述熱可塑性樹脂發泡粒子於模内發泡成形， 而製得熱可塑性樹脂發泡成形體之步驟。 ® 12. —種發泡性熱可塑性樹脂粒子，係為藉由申請專利範 圍第8項之發泡性熱可塑性樹脂粒子的製造方法所製 得者。 13. —種熱可塑性樹脂發泡粒子，係為使申請專利範圍第 12項之發泡性熱可塑性樹脂粒子預發泡所製得者。 14. 一種熱可塑性樹脂發泡成形體，係為使申請專利範圍 第13項之熱可塑性樹脂發泡粒子於模内發泡成形所製 赢 得者。 41 321055修正版• Patent Application No. 9810^224, October 26, 100, revised replacement page, 1359068 ----| 咏私月绔 (French &gt; is replacing the Department. «. i "》·&gt;· -^ «» *» , · -· · VII. Application for profit-seeking range::;:: 1. Two types of granulation molds are characterized by: a resin discharge surface provided in contact with a refrigerant; connected to a resin supply device a plurality of resin flow paths; a nozzle that communicates with the resin flow path and forms an opening in the resin discharge surface; and a plurality of insertion heating ports and ports provided in the vicinity of the resin discharge surface, and the resin flow path Arranging along the circumference of the virtual circle on the resin discharge surface; the insertion heater is disposed on both sides of the circumference of the circumference of each of the plurality of resin flow paths, and has a length direction toward the circumference 2. The granulation mold according to the first aspect of the invention, wherein the insert heater is provided in a plurality of or more; and the center angle of each of the cartridge heaters is 45. ° below. φ 3. If you apply for The granulation mold according to the first aspect of the invention, wherein the inserting heater is provided at a position of 10 to 50 mm from the resin discharge surface. The cross-sectional shape of the resin flow path is such that the outer contour has a straight portion; the straight portion is disposed substantially parallel to the longitudinal direction of the insert heater. 5. The granulation mold according to the first aspect of the patent application, wherein </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> <RTIgt; </ RTI> </ RTI> </ RTI> </ RTI> </ RTI> </ RTI> </ RTI> </ RTI> <RTIgt; The mold is characterized in that temperature sensing is provided on at least the upstream side and the downstream side of the flow direction of the refrigerant, and the plug-in heater is individually controlled to be switched based on the measured temperature of the temperature sensor. A granulation apparatus comprising: the granulation mold according to any one of claims 1 to 6; and the resin for mounting the granulation mold at the front end And a processing chamber in which the resin which is discharged from the nozzle of the granulation mold is cut, and the refrigerant is brought into contact with the resin discharge surface of the granulation mold. A method for producing a plastic resin particle, comprising: φ a step of supplying a thermoplastic resin to a resin supply device to which a granulation mold according to any one of claims 1 to 6 is attached, and performing melt-kneading; a step of injecting a foaming agent into the thermoplastic resin to form a resin containing a foaming agent while moving the thermoplastic resin toward the granulation mold; and using a cutter to granulate the granule in the refrigerant The foaming agent-containing resin discharged from the nozzle of the mold is cut to obtain a foamable thermoplastic resin particle. 39 321 055 修正 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 The temperature of the mold on the upstream side and the downstream side in the water flow direction is individually controlled to be switched on and off for each of the sheathed heaters so that the respective measured values are equal. 10. A method of producing a thermoplastic resin foamed particle, comprising: supplying a thermoplastic resin to a resin supply device in which a granulation mold according to any one of claims 1 to 6 is attached, and a step of performing melt-kneading; β a step of injecting a foaming agent into the thermoplastic resin to form a resin containing a foaming agent while moving the thermoplastic resin toward the granulation mold; and using a cutter in the refrigerant a step of cutting the foaming agent-containing resin discharged from the nozzle of the granulation mold to obtain foamable thermoplastic resin particles, and pre-expanding the foamable thermoplastic resin particles. Thus, 0 thermoplastic resin expanded particles were obtained. A method of producing a thermoplastic resin foamed molded article, comprising: supplying a thermoplastic resin to a resin supply device to which a granulation mold according to any one of claims 1 to 6 is attached, and a step of melt-kneading; the foaming agent is injected into the thermoplastic resin while moving the thermoplastic resin toward the granulation mold to form a 40 321 055 modified version 1359068 _ 98,102,224 patent application; 100 years 10 On the 26th of the month, the step of replacing the resin having the foaming agent is replaced; and the foaming agent-containing resin discharged from the nozzle of the granulating mold is cut by a cutter in a refrigerant to obtain a hair- a step of foaming the thermoplastic resin particles; heating the foamable thermoplastic resin particles to pre-expand them to obtain thermoplastic resin foamed particles; and foaming the thermoplastic resin foam particles in the mold. The step of producing a thermoplastic resin foam molded body is obtained. ® 12. A foamable thermoplastic resin particle obtained by the method for producing foamable thermoplastic resin particles of the eighth application of the patent application. A thermoplastic resin foamed particle obtained by pre-expanding the foamable thermoplastic resin particles of claim 12 of the patent application. A thermoplastic resin foam molded article obtained by subjecting the thermoplastic resin foamed particles of claim 13 to in-mold foam molding. 41 321055 revision
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